CN203998980U - The system that ammonia is produced in a kind of urea soln hydrolysis - Google Patents
The system that ammonia is produced in a kind of urea soln hydrolysis Download PDFInfo
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- CN203998980U CN203998980U CN201420250462.4U CN201420250462U CN203998980U CN 203998980 U CN203998980 U CN 203998980U CN 201420250462 U CN201420250462 U CN 201420250462U CN 203998980 U CN203998980 U CN 203998980U
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Abstract
The system that ammonia is produced in a kind of urea soln hydrolysis, it comprises hydrolyzer, hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, hydrophobic heat exchanger, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, vapor heat exchanger, hydrolysis gas temperature out meter T2, hydrolysis gas rate of discharge meter F, steam trap and hydrolysis system control module, hydrolyzer is provided with 7 interfaces, connects respectively above-mentioned; Hydrolysis system control module is connected with hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, hydrolysis gas temperature out meter T2 and hydrolysis gas rate of discharge meter F respectively by cable; The utility model is simple and reliable, controls flexible.Thermal source owing to adopting steam as hydrolysis system, greatly reduces running cost.Its no coupling product produces, so non-secondary pollution.
Description
Technical field
The utility model relates to the system that ammonia is produced in a kind of urea soln hydrolysis, and it is applicable to provide for equipment for denitrifying flue gas the preparation system of denitrification reducing agent (ammonia).SCR (SCR) gas denitrifying technology that belongs to environmental technology field.
Background technology
The atmospheric polluting material producing after coal combustion mainly contains sulfurous gas, oxynitride, flue dust (pellet) and as the carbonic acid gas of greenhouse gases.Due to coal fire discharged and vehicular emission, the pollution of the oxynitride of China is very serious.
In recent years, raising gradually along with 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.
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 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 of its total liquefied ammonia in source, ammoniacal liquor and urea solns, urea soln ammonia process processed, due to reasons such as its safety performance are good, urea convenient sources, has obtained the application of wide at present.
Urea soln is prepared ammonia two kinds of pyrolysis method and hydrolysis method, and pyrolysis method, under normal pressure and high temperature (350～600 ℃), makes urea soln be decomposed into ammonia, water vapour and carbonic acid gas.Pyrolysis method is because medium temperature is high, so energy consumption is larger, and pyrolysis method must configure separately pyrolysis system by every boiler, so cost of investment is also higher.And the operational condition of hydrolysis method is middle pressure (0.4～1.0MPa) and middle temperature (120～200 ℃), in hydrolyzer, make urea soln be decomposed into ammonia, water vapour and carbonic acid gas.Because its service temperature is lower, energy consumption is less, and can use cost lower steam is as heat source, therefore greatly reduces running cost.The load regulation range of hydrolyzer is larger, can many public hydrolyzer of boiler, thereby also greatly reduce cost of investment, be with a wide range of applications.
Utility model content
1, object: the purpose of this utility model is to provide the system that ammonia is produced in a kind of urea soln hydrolysis.The urea soln that enters system, first by hydrophobic heat exchanger, utilizes the waste heat of steam drainage, by the temperature of urea soln by～40 ℃ rise to～100 ℃, then enter hydrolyzer.In hydrolyzer, by steam heating, the pressure and temperature of urea soln is promoted to the level of middle pressure (0.4～1.0MPa) and middle temperature (120～200 ℃), under this temperature and pressure, hydrolysis of urea is ammonia and carbonic acid gas, and water is also evaporated to water vapour simultaneously, discharges hydrolyzer.The hydrolysis gas of discharging hydrolyzer is saturation steam, and its component comprises ammonia, water vapour and carbonic acid gas.Hydrolysis gas, first by variable valve, by pressure decreased to 0.1～0.4MPa, then by vapor heat exchanger, improves 30～50 ℃ by the temperature of hydrolysis gas, to prevent that ammonia reversed reaction from generating urea or biuret.Then as denitrification reducing agent, be sent to SCR denitrating system.Enter the superheated vapour of system first by vapor heat exchanger, after heating water is vented one's spleen, its temperature is reduced to and approaches or the temperature that reaches capacity, and then delivers to hydrolyzer, for providing thermal source to hydrolyzer.From hydrolyzer steam drainage out, enter hydrophobic heat exchanger, utilize hydrophobic waste heat, the urea soln of heating import.Hydrophobic discharge system after utilization, can store, for the configuration of urea soln.The generation of whole system non-secondary pollution.
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 urea soln hydrolysis, it is characterized in that, it comprises hydrolyzer, hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, hydrophobic heat exchanger, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, vapor heat exchanger, hydrolysis gas temperature out meter T2, hydrolysis gas rate of discharge meter F, steam trap and hydrolysis system control module, sees Fig. 1.Position annexation between them is: it is N1～N7 interface that hydrolyzer is provided with 7 interfaces, is described below respectively:
N1 interface connects urea soln inlet pipeline, for supplying raw materials to hydrolyzer---and urea soln.On urea soln inlet pipeline, be provided with successively urea soln variable valve A1 and hydrophobic heat exchanger.
N2 interface connects hydrolysis gas outlet conduit, for outwards carrying ammonia.On hydrolysis gas outlet conduit, be provided with successively hydrolysis gas outlet regulating valve A3, vapor heat exchanger, hydrolysis gas temperature out meter T2 and hydrolysis gas rate of discharge meter F.
N3 interface connects heating steam inlet pipeline, for providing thermal source to hydrolyzer.On steam inlet pipeline, be provided with successively steam regulating valve A2 and vapor heat exchanger.
N4 interface connects steam drainage outlet conduit, for discharging steam drainage.On steam drainage outlet conduit, be provided with successively steam trap and hydrophobic heat exchanger.
N5 interface connects hydrolyzer thermometer T1, for measuring the operating temperature in hydrolyzer.
N6 interface connects hydrolyzer pressure unit P, for measuring the operating pressure in hydrolyzer.
N7 interface connects hydrolyzer liquidometer L, for measuring the operation liquid level in hydrolyzer.
Hydrolysis system control module is connected with hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, hydrolysis gas temperature out meter T2 and hydrolysis gas rate of discharge meter F respectively by cable.Hydrolysis system control module is connected by communication cable with SCR denitration Controlling System simultaneously, from SCR denitration Controlling System, obtains the required ammonia flow of SCR denitrating system.
This hydrolyzer is BKU type kettle-type reboiler, and thermal source adopts saturation steam, and inside is provided with U-shaped tube bank steam heating tube, and the heat interchanging area of steam heating tube and the cubic capacity of hydrolyzer are determined according to the ammonia turnout of specified hydrolyzer.
This vapor heat exchanger is vertical array tubular interchanger, and thermal source adopts superheated vapour, and inside is provided with shell and tube steam heating tube, and the heat interchanging area of steam heating tube is determined according to the rated flow of hydrolysis gas and temperature rise.Superheated vapour is by after vapor heat exchanger, and its design variable reaches or approaches saturation steam.
This hydrophobic heat exchanger is vertical array tubular interchanger, and thermal source adopts steam drainage, and inside is provided with the hydrophobic heating tube of shell and tube, and the heat interchanging area of hydrophobic heating tube is determined according to the rated flow of urea soln and temperature rise.
This urea soln variable valve A1, steam regulating valve A2 and hydrolysis gas outlet regulating valve A3 are the pneumatic or motor-driven control valve of explosion-proof type.
This hydrolyzer pressure unit P is Anti-explosion intelligent pressure unit.
This hydrolyzer thermometer T1 and hydrolysis gas temperature out meter T2 are explosion-proof type PT100 type platinum resistance thermometer sensor,s (two armourings).
This hydrolyzer rate of discharge meter F is explosion-proof type Coriolis flowmeter.
This hydrolyzer liquidometer L is explosion-proof type two wire system static pressure tubular type radar level gauge.
This steam trap is free floating-ball type steam draining valve.
This hydrolysis system control module adopts PLC or DCS Controlling System.
(2) control method that ammonia is produced in urea soln hydrolysis, the method is specifically controlled step and is:
Step 1: by regulating the aperture of urea soln variable valve A1, adjust the urea flow that enters hydrolyzer, thereby the indicating value of controlled hydrolysis device liquidometer L is stable.If hydrolyzer operation liquid level, lower than set(ting)value, increases the aperture of urea soln variable valve A1, thereby increases the inlet of urea soln; If hydrolyzer operation liquid level, higher than set(ting)value, reduces the aperture of urea soln variable valve A1, thereby reduces the inlet of urea soln.
Step 2: by the aperture of steam regulation variable valve A2, adjust the steam flow that enters hydrolyzer, thereby the indicating value of controlled hydrolysis actuator temperature meter T1 is stable.If hydrolyzer operating temperature, lower than set(ting)value, increases the aperture of steam regulating valve A2, thus the inlet of increase steam; If hydrolyzer operating 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 hydrolysis gas rate of discharge meter F obtains by SCR (SCR) denitrating flue gas Controlling System.By adjusting, be hydrolyzed the aperture of gas outlet regulating valve A3, obtain the required ammonia flow of SCR (SCR) flue gas denitrification system, be hydrolyzed the flow of gas.If hydrolysis airshed lower than set(ting)value, increases the aperture of hydrolysis gas outlet regulating valve A3, thereby increases hydrolysis airshed; If hydrolysis airshed, higher than set(ting)value, reduces to be hydrolyzed the aperture of gas outlet regulating valve A3, thereby reduce hydrolysis airshed.
Step 4: the indicating value of hydrolyzer pressure unit P is controlled by hydrolyzer thermometer T1.In hydrolyzer, belong to gas-liquid two-phase, operating pressure is the saturation pressure under operating temperature.In operational process, along with the ammonia turnout variation of hydrolyzer, operating pressure will have certain fluctuation.If operating pressure is starkly lower than saturation pressure, illustrate that hydrolyzer has leakage; If operating pressure apparently higher than saturation pressure, illustrates that instrument measurement has fault, as liquidometer fault etc.Therefore the deviation of working as operating pressure and theoretical saturation pressure is higher than set(ting)value, and hydrolysis system control module will propose to report to the police, and require hydrolyzer parking maintenance.
Step 5: the discharge of steam drainage is that steam trap is realized automatically.By steam trap, steam condensate is discharged outside hydrolyzer, and steam continues to stay heat exchange in hydrolyzer.
Step 6: hydrolysis system provides Real-Time Monitoring to the observed value of hydrolysis gas temperature out meter T2, require the superheating temperature of outlet hydrolysis gas higher than set(ting)value (temperature of saturation is hydrolyzer operating temperature), when the superheating temperature of hydrolysis gas is during lower than set(ting)value, hydrolysis system control module will propose warning.
Wherein, the set(ting)value of the hydrolyzer described in step 1 operation liquid level be hydrolyzer the highest liquid level 50%.
Wherein, the set(ting)value of the hydrolyzer operating temperature described in step 2 is 120～200 ℃, and corresponding saturation pressure is 0.4～1.0MPa.
Wherein, the set(ting)value of the hydrolyzer rate of discharge described in step 3 is obtained from SCR denitration Controlling System.
Wherein, the deviation setting value of the hydrolyzer operating pressure described in step 4 and theoretical saturation pressure is 0.2MPa.
Wherein, the set(ting)value of the hydrolysis of the outlet described in step 6 gas superheating temperature is 30～50 ℃.
3, advantage and effect: the utility model system is simple and reliable, control flexible.Thermal source owing to adopting steam as hydrolysis system, greatly reduces running cost.Owing to having increased vapor heat exchanger on hydrolysis gas outlet line, improved on the one hand the temperature of hydrolysis gas, avoided hydrolysis gas in growing apart from course of conveying, the ammonia reversed reaction causing lower than temperature of saturation due to temperature, produce the materials such as urea or biuret, therefore greatly reduced the dew point corrosion risk in follow-up pipeline and equipment.On the other hand because hydrolyzer need to use saturation steam, and superheated vapour has passed through after vapor heat exchanger, and its parameter has approached or the steam that reaches capacity, and can directly enter hydrolyzer, has avoided use steam temperature reducing and pressure reducing device.Owing to having increased hydrophobic heat exchanger in urea soln inlet line, improve the inlet temperature of urea soln simultaneously, reclaimed hydrophobic waste heat simultaneously, be conducive to improve the utilising efficiency of the energy, reduced energy consumption.The utility model no coupling product produces, so non-secondary pollution.
Accompanying drawing explanation
Fig. 1 is the utility model system architecture schematic diagram;
1., hydrolyzer in figure, nomenclature is as follows:; 2., hydrolyzer thermometer T1; 3., hydrolyzer transmitter P; 4., hydrolyzer liquidometer L; 5., urea soln variable valve A1; 6., hydrophobic heat exchanger; 7., steam regulating valve A2; 8., hydrolysis gas outlet regulating valve A3; 9., vapor heat exchanger; 10., hydrolysis gas temperature out meter T2, (11), hydrolysis gas rate of discharge meter F, (12), steam trap; N1-N7 interface is 7 pipe joint positions that hydrolyzer 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 urea soln hydrolysis, it is characterized in that, it comprise hydrolyzer 1., hydrolyzer thermometer T1 2., hydrolyzer pressure unit P 3., hydrolyzer liquidometer L 4., urea soln variable valve A1 5., hydrophobic heat exchanger 6., steam regulating valve A2 7., hydrolysis gas outlet regulating valve A3 8., vapor heat exchanger 9., hydrolysis gas temperature out meter T2 10., hydrolysis gas rate of discharge meter F (11), steam trap (12) and hydrolysis system control module.Position annexation between them is: 1. hydrolyzer is provided with 7 interfaces is N1～N7 interface, is described below respectively:
N1 interface connects urea soln inlet pipeline, for 1. supplying raw materials to hydrolyzer---and urea soln.On urea soln inlet pipeline, be provided with successively urea soln variable valve A1 5. with hydrophobic heat exchanger 6..
N2 interface connects hydrolysis gas outlet conduit, for outwards carrying ammonia.On hydrolysis gas outlet conduit, be provided with successively hydrolysis gas outlet regulating valve A3 8., vapor heat exchanger 9., hydrolysis gas temperature out meter T2 10. with hydrolysis gas rate of discharge meter F (11).
N3 interface connects heating steam inlet pipeline, for 1. providing thermal source to hydrolyzer.On steam inlet pipeline, be provided with successively steam regulating valve A2 7. with vapor heat exchanger 9..
N4 interface connects steam drainage outlet conduit, for discharging steam drainage.On steam drainage outlet conduit, be provided with successively steam trap (12) and hydrophobic heat exchanger 6..
2. N5 interface connects hydrolyzer thermometer T1, for measuring the operating temperature in hydrolyzer.
3. N6 interface connects hydrolyzer pressure unit P, for measuring the operating pressure in hydrolyzer.
4. N7 interface connects hydrolyzer liquidometer L, for measuring the operation liquid level in hydrolyzer.
Hydrolysis system control module by cable respectively with hydrolyzer thermometer T1 2., hydrolyzer pressure unit P 3., hydrolyzer liquidometer L 4., urea soln variable valve A1 5., steam regulating valve A2 7., hydrolysis gas outlet regulating valve A3 8., 10. hydrolysis gas temperature out meter T2 be connected with hydrolysis gas rate of discharge meter F (11).Hydrolysis system control module is connected by communication cable with SCR denitration Controlling System simultaneously, from SCR denitration Controlling System, obtains the required ammonia flow of SCR denitrating system.
1. this hydrolyzer is BKU type kettle-type reboiler, and thermal source adopts saturation steam, and inside is provided with U-shaped tube bank steam heating tube, and the heat interchanging area of steam heating tube and the cubic capacity of hydrolyzer are determined according to hydrolyzer ammonia rated output 1..
9. this vapor heat exchanger is vertical array tubular interchanger, and thermal source adopts superheated vapour, and inside is provided with shell and tube steam heating tube, and the heat interchanging area of steam heating tube is determined according to the rated flow of hydrolysis gas and temperature rise.Superheated vapour by vapor heat exchanger 9. after, its design variable reaches or approaches saturation steam.
6. this hydrophobic heat exchanger is vertical array tubular interchanger, and thermal source adopts steam drainage, and inside is provided with the hydrophobic heating tube of shell and tube, and the heat interchanging area of hydrophobic heating tube is determined according to the rated flow of urea soln and temperature rise.
This urea soln variable valve A1 5., 8. 7. steam regulating valve A2 be the pneumatic or motor-driven control valve of explosion-proof type with hydrolysis gas outlet regulating valve A3.
3. this hydrolyzer pressure unit P is Anti-explosion intelligent pressure unit.
10. 2. this hydrolyzer thermometer T1 be explosion-proof type PT100 type platinum resistance thermometer sensor, (two armourings) with hydrolysis gas temperature out meter T2.
This hydrolyzer rate of discharge meter F (11) is explosion-proof type Coriolis flowmeter.
4. this hydrolyzer liquidometer L is explosion-proof type two wire system static pressure tubular type radar level gauge.
This steam trap (12) is free floating-ball type steam draining valve.
This hydrolysis system control module adopts PLC or DCS Controlling System.
(2) control method that ammonia is produced in urea soln hydrolysis, the method is specifically controlled step and is:
Step 1: by regulating urea soln variable valve A1 aperture 5., adjust and enter hydrolyzer urea flow 1., thereby controlled hydrolysis device liquidometer L indicating value is 4. stable.If 1. hydrolyzer moves liquid level lower than set(ting)value, increase urea soln variable valve A1 aperture 5., thereby increase the inlet of urea soln; If 1. hydrolyzer moves liquid level higher than set(ting)value, reduce urea soln variable valve A1 aperture 5., thereby reduce the inlet of urea soln.
Step 2: by steam regulation variable valve A2 aperture 7., adjust and enter hydrolyzer steam flow 1., thereby controlled hydrolysis actuator temperature meter T1 indicating value is 2. stable.If hydrolyzer 1. operating temperature, lower than set(ting)value, increases steam regulating valve A2 aperture 7., thus the inlet of increase steam; If hydrolyzer 1. operating temperature, higher than set(ting)value, reduces steam regulating valve A2 aperture 7., thus the inlet of minimizing steam.
Step 3: the set(ting)value of hydrolysis gas rate of discharge meter F (11) obtains by SCR (SCR) denitrating flue gas Controlling System.By adjusting, be hydrolyzed gas outlet regulating valve A3 aperture 8., obtain the required ammonia flow of SCR (SCR) flue gas denitrification system, be hydrolyzed the flow of gas.If hydrolysis airshed lower than set(ting)value, increases hydrolysis gas outlet regulating valve A3 aperture 8., thereby increases hydrolysis airshed; If hydrolysis airshed, higher than set(ting)value, reduces to be hydrolyzed gas outlet regulating valve A3 aperture 8., thereby reduce hydrolysis airshed.
Step 4: 2. hydrolyzer pressure unit P indicating value is 3. controlled by hydrolyzer thermometer T1.In hydrolyzer, belong to gas-liquid two-phase, operating pressure is the saturation pressure under operating temperature.In operational process, along with hydrolyzer ammonia turnout 1. changes, operating pressure will have certain fluctuation.If operating pressure is starkly lower than saturation pressure, illustrate that 1. hydrolyzer has leakage; If operating pressure apparently higher than saturation pressure, illustrates that instrument measurement has fault, as liquidometer fault etc.Therefore the deviation of working as operating pressure and theoretical saturation pressure is higher than set(ting)value, and hydrolysis system control module will propose to report to the police, and require 1. parking maintenance of hydrolyzer.
Step 5: the discharge of steam drainage is that steam trap (12) is realized automatically.By steam trap (12), steam condensate discharge hydrolyzer 1. outside, steam continue to stay hydrolyzer 1. in heat exchange.
Step 6: hydrolysis system provides Real-Time Monitoring to hydrolysis gas temperature out meter T2 observed value 10., require the superheating temperature of outlet hydrolysis gas higher than set(ting)value (temperature of saturation is 1. operating temperature of hydrolyzer), when the superheating temperature of hydrolysis gas is during lower than set(ting)value, hydrolysis system control module will propose warning.
Wherein, the hydrolyzer described in step 1 1. move the set(ting)value of liquid level be hydrolyzer the highest liquid level 50%.
Wherein, the hydrolyzer described in the step 2 1. set(ting)value of operating temperature is 120～200 ℃, and corresponding saturation pressure is 0.4～1.0MPa.
Wherein, the hydrolyzer described in step 3 1. the set(ting)value of rate of discharge from SCR denitration Controlling System, obtain.
Wherein, the hydrolyzer described in step 4 1. the deviation setting value of operating pressure and theoretical saturation pressure be 0.2MPa.
Wherein, the set(ting)value of the hydrolysis of the outlet described in step 6 gas superheating temperature is 30～50 ℃.
Claims (1)
1. the system that ammonia is produced in urea soln hydrolysis, is characterized in that: it comprises hydrolyzer, hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, hydrophobic heat exchanger, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, vapor heat exchanger, hydrolysis gas temperature out meter T2, hydrolysis gas rate of discharge meter F, steam trap and hydrolysis system control module; It is N1～N7 interface that hydrolyzer is provided with 7 interfaces, connects respectively as follows:
N1 interface connects urea soln inlet pipeline, is provided with successively urea soln variable valve A1 and hydrophobic heat exchanger on urea soln inlet pipeline;
N2 interface connects hydrolysis gas outlet conduit, is provided with successively hydrolysis gas outlet regulating valve A3, vapor heat exchanger, hydrolysis gas temperature out meter T2 and hydrolysis gas rate of discharge meter F on hydrolysis gas outlet conduit;
N3 interface connects heating steam inlet pipeline, is provided with successively steam regulating valve A2 and vapor heat exchanger on steam inlet pipeline;
N4 interface connects steam drainage outlet conduit, is provided with successively steam trap and hydrophobic heat exchanger on steam drainage outlet conduit;
N5 interface connects hydrolyzer thermometer T1;
N6 interface connects hydrolyzer pressure unit P;
N7 interface connects hydrolyzer liquidometer L;
Hydrolysis system control module is connected with hydrolyzer thermometer T1, hydrolyzer pressure unit P, hydrolyzer liquidometer L, urea soln variable valve A1, steam regulating valve A2, hydrolysis gas outlet regulating valve A3, hydrolysis gas temperature out meter T2 and hydrolysis gas rate of discharge meter F respectively by cable; Hydrolysis system control module is connected by communication cable with SCR denitration Controlling System simultaneously;
This hydrolyzer is kettle-type reboiler, and thermal source adopts saturation steam, and inside is provided with U-shaped tube bank steam heating tube;
This vapor heat exchanger is vertical array tubular interchanger, and thermal source adopts superheated vapour, and inside is provided with shell and tube steam heating tube, and superheated vapour is by after vapor heat exchanger, and its design variable reaches or approaches saturation steam;
This hydrophobic heat exchanger is vertical array tubular interchanger, and thermal source adopts steam drainage, and inside is provided with the hydrophobic heating tube of shell and tube;
This urea soln variable valve A1, steam regulating valve A2 and hydrolysis gas outlet regulating valve A3 are the pneumatic or motor-driven control valve of explosion-proof type;
This hydrolyzer pressure unit P is Anti-explosion intelligent pressure unit;
This hydrolyzer thermometer T1 and hydrolysis gas temperature out meter T2 are explosion-proof type platinum resistance thermometer sensor,s;
This hydrolyzer rate of discharge meter F is explosion-proof type Coriolis flowmeter;
This hydrolyzer liquidometer L is explosion-proof type two wire system static pressure tubular type radar level gauge;
This steam trap is free floating-ball type steam draining valve;
This hydrolysis system control module adopts PLC or DCS Controlling System.
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| CN201420250462.4U CN203998980U (en) | 2014-05-16 | 2014-05-16 | The system that ammonia is produced in a kind of urea soln hydrolysis |
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| CN201420250462.4U CN203998980U (en) | 2014-05-16 | 2014-05-16 | The system that ammonia is produced in a kind of urea soln hydrolysis |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104909386A (en) * | 2015-05-25 | 2015-09-16 | 成都锐思环保技术股份有限公司 | Urea hydrolysis ammonia-production equipment and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104909386A (en) * | 2015-05-25 | 2015-09-16 | 成都锐思环保技术股份有限公司 | Urea hydrolysis ammonia-production equipment and method |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141210 Termination date: 20160516 |
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| CF01 | Termination of patent right due to non-payment of annual fee |