CN109279625A - Urea hydrolysis ammonia producing system and its hydrolysis ammonia method processed - Google Patents
Urea hydrolysis ammonia producing system and its hydrolysis ammonia method processed Download PDFInfo
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- CN109279625A CN109279625A CN201811467952.9A CN201811467952A CN109279625A CN 109279625 A CN109279625 A CN 109279625A CN 201811467952 A CN201811467952 A CN 201811467952A CN 109279625 A CN109279625 A CN 109279625A
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- Prior art keywords
- urea
- ammonia
- dissolution
- hydrolysis
- liquid
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 194
- 239000004202 carbamide Substances 0.000 title claims abstract description 159
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 157
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 128
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 128
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000004090 dissolution Methods 0.000 claims abstract description 79
- 238000010438 heat treatment Methods 0.000 claims abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 238000005507 spraying Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims description 102
- 239000000203 mixture Substances 0.000 claims description 20
- 239000008187 granular material Substances 0.000 claims description 12
- 238000010790 dilution Methods 0.000 claims description 8
- 239000012895 dilution Substances 0.000 claims description 8
- 238000004065 wastewater treatment Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 4
- 230000006837 decompression Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 4
- 239000013529 heat transfer fluid Substances 0.000 claims description 3
- 239000006193 liquid solution Substances 0.000 claims 1
- 239000002245 particle Substances 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000000243 solution Substances 0.000 description 20
- 239000007789 gas Substances 0.000 description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 4
- 239000000908 ammonium hydroxide Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- PPBAJDRXASKAGH-UHFFFAOYSA-N azane;urea Chemical compound N.NC(N)=O PPBAJDRXASKAGH-UHFFFAOYSA-N 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 210000002700 urine Anatomy 0.000 description 3
- 238000010612 desalination reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- WTHDKMILWLGDKL-UHFFFAOYSA-N urea;hydrate Chemical compound O.NC(N)=O WTHDKMILWLGDKL-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/08—Preparation of ammonia from nitrogenous organic substances
- C01C1/086—Preparation of ammonia from nitrogenous organic substances from urea
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of urea hydrolysis ammonia producing systems.It includes urea dissolution/holding vessel, the steam stream that steam-heating system generates is divided into two strands, one steam stream is passed through in heating coil by connecting pipeline, heating coil is located in hydrolysis reactor, another burst of steam stream is passed through stripped vapor spraying system by connecting pipeline, and stripped vapor spraying system is located at the bottom of hydrolysis reactor；Heating coil water outlet is connected to dissolution heating tube, and dissolution heating tube is located in urea dissolution/holding vessel；Urea dissolution/holding vessel water outlet lead to water inlet connecting pipeline on be successively arranged circulation conveying pump, the second solenoid electric valve；Urea dissolution/holding vessel is equipped with the connecting pipeline towards hydrolysis reactor；Hydrolysis reactor upper end is connected to nozzle, and nozzle is passed through ammonia mixer.The present invention has the advantages that low energy consumption, ammonia high conversion rate, at low cost.The invention also discloses urea hydrolysis ammonia producing systems to hydrolyze ammonia method processed.
Description
Technical field
The present invention relates to technical field of air pollution control, more specifically say it is urea hydrolysis ammonia producing system.More specifically
Ground says it is a kind of system that hydrolysis of urea ammonia is used for flue gas SCR (selective catalytic reduction system operating) denitration.The present invention also relates to
And urea hydrolysis ammonia producing system hydrolyzes ammonia method processed.
Background technique
China's power supply is based on coal-fired thermal power generation, and heat power plant boiler burning generates a large amount of flue gas,
Wherein the oxynitrides NOx of NOx is the major pollutants for causing photochemical fog and acid rain.Formally implement within 2012 " fire
Power plant's atmosphere pollutants emission standards " it requires, all fossil fuel fired boilers must be provided with denitrification apparatus, to control NOx pairs
The influence of environment.
And most common SCR denitration process technology is under the action of metallic catalyst, using ammonia by the NOx in flue gas
Also original production N2, to realize the qualified discharge of NOx.
The method for preparing ammonia at present mainly has liquefied ammonia/ammonium hydroxide ammonia, urea pyrolysis ammonia, the side such as hydrolysis of urea ammonia
Method.Liquefied ammonia/ammonium hydroxide belongs to dangerous material, and there are biggish risks in transport and storage.Urea is a kind of colourless chemicals, easily
In transport, storage is highly suitable as the raw materials for production of ammonia, but urea pyrolysis ammonia equipment is asked there are operating cost is higher
Topic, hydrolysis of urea have operation energy consumption low, safety, and stable feature increasingly receives an acclaim.
Existing Chinese Patent Application No. is 201710151844.X, and patent name is a kind of " urea seeding using waste heat
Hydrolyze ammonia system and method processed ", this method uses heat source of the hot-air as ammonium hydroxide solution, because the heat enthalpy value of hot-air is opposite
Small, the air quantity needed is big, thereby increases and it is possible to which there are hydrolysis to be not thorough, the slower problem of hydrolytic process；
Existing Chinese Patent Application No. is 201410490482.3, and patent name is a kind of " urea using boiler gas
Hydrolyze ammonia method and apparatus processed ", the heat source using boiler smoke as ammonium hydroxide solution, there are smoke components complexity (containing flying dust,
SO2Deng), after being passed through hydrolysis system, impurity can be generated, impurity cannot be excluded effectively, influence the use of hydrolytic decomposition pot, cause spray ammonia logical
The problems such as road blocks.
Current hydrolysis of urea system mostly uses the high-quality steam of power plant to be heated, but that there are heat utilization ratios is low,
The problems such as use cost is high.
Therefore, now need to research and develop that a kind of heating efficiency is higher, and low energy consumption, ammonia high conversion rate, urea water at low cost
Solution ammonia system and its hydrolysis ammonia method processed.
Summary of the invention
The first object of the present invention is to provide for a kind of urea hydrolysis ammonia producing system, and heating efficiency is higher, energy consumption
Low, ammonia high conversion rate is at low cost, overcomes heating efficiency in prior art technology not high, and it is direct to solve hydrolysis of urea waste liquid
The problem of waste caused by exhausting and pollution.
The second object of the present invention is to provide for a kind of urea hydrolysis ammonia producing system hydrolysis ammonia method processed, easy to operate,
Ammonia high conversion rate.
In order to realize the first purpose of aforementioned present invention, the technical solution of the present invention is as follows: urea hydrolysis ammonia producing system, special
Sign is: the steam stream generated including urea dissolution/holding vessel, hydrolysis reactor and steam-heating system, steam-heating system
It is divided into two strands, one steam stream is passed through in heating coil by connecting pipeline, and the heating coil is located at the hydrolysis reactor
Interior, another burst of steam stream is passed through stripped vapor spraying system by connecting pipeline, and the stripped vapor spraying system is located at described
The bottom of hydrolysis reactor；
The heating coil water outlet is connected to by connecting pipeline with dissolution heating tube, and the dissolution heating tube is located at described
In urea dissolution/holding vessel；
Urea dissolution/holding vessel the water outlet is equipped with the first connecting pipeline of connection water inlet, first connection
Circulation conveying pump and the second solenoid electric valve are successively arranged on pipeline；
There is hydrolysis reactor water inlet to be set to the hydrolysis reactor lower end, the urea dissolution/holding vessel, which is equipped with, to be connected
Lead to the second connecting pipeline of the hydrolysis reactor；The circulation conveying pump, first are successively arranged on second connecting pipeline
Solenoid electric valve and energy-saving heat exchanger；
The hydrolysis reactor lower end is equipped with hydrolysis reactor liquid outlet, and the hydrolysis reactor liquid outlet is logical
It crosses third connecting pipe to be connected with gas-liquid separator, the third connecting pipe is connected with the energy-saving heat exchanger；
The gas-liquid separator upper end is equipped with gas discharge outlet, and the gas discharge outlet is connected with the ammonia mixer
Logical, lower end is equipped with gas-liquid separator liquid outlet, the gas-liquid separator liquid outlet and the urea dissolution/holding vessel
It is connected；
The hydrolysis reactor upper end is connected to nozzle, and the nozzle is passed through ammonia mixer；Dilution air passes through connection
Pipeline is connected with the ammonia mixer；The ammonia mixer is equipped with the pipeline towards flue denitrating system.
In the above-mentioned technical solutions, the connecting pipeline of the gas-liquid separator and the urea dissolution/holding vessel is equipped with
Third solenoid electric valve.
In the above-mentioned technical solutions, the water inlet of the urea dissolution/holding vessel is set to the top of water outlet.
In the above-mentioned technical solutions, the dissolution heating tube water outlet is connected to by connecting pipeline with waste water treatment system.
In the above-mentioned technical solutions, the steam stream that the steam-heating system generates is passed through on the connecting pipeline of heating coil
Equipped with cooling decompression device.
In order to realize the second purpose of aforementioned present invention, the technical solution of the present invention is as follows: the hydrolysis of urea ammonia system
System hydrolyzes ammonia method processed, characterized by the following steps:
S1: the urea granules in urea system are added to urea by corresponding entrance with the demineralized water in DW system demineralized water system
In dissolution/holding vessel, urea granules are configured to 40%~60% urea liquid；
S2: the condensate liquid of heating coil is passed through the dissolution heating tube in urea dissolution/holding vessel, urea in hydrolysis reactor
It is 40 DEG C that urea liquid in dissolution/holding vessel, which passes through dissolution heating tube and condensed heat transfer fluid to temperature, dissolution heating tube water outlet
Into waste water treatment system；
S3: circulation conveying pump promotes circulation of the urea liquid in pipeline, accelerates course of dissolution, by the urea liquid of dissolution
Deliver into hydrolysis of urea system；
S4: the urea liquid on the second connecting pipeline is increased to 160 DEG C from 40 DEG C by the energy-saving heat exchanger on transfer pipeline
~180 DEG C；
S5: the hydrolysis in hydrolysis reactor is controlled by steam-heating system, the hydrolysis in hydrolysis reactor
Temperature is 150 DEG C~170 DEG C, and pressure is 1.8Mpa~2.1Mpa；
S6: the stripped vapor spraying system of hydrolysis reactor bottom setting takes away ammonia gas mixture；
S7: hydrolysis reactor is discharged by nozzle in the ammonia gas mixture generated in hydrolysis reactor, and ammonia gas mixture passes through
Nozzle is sent into ammonia mixer；
S8: air is sent into ammonia mixer by dilution air, is 30%~35% by ammonia level in ammonia mixer
Ammonia gas mixture be diluted to ammonia level be 5% after, be sent into flue denitrating system；
S9: the poor urea liquid generated after hydrolysis is discharged by hydrolysis reactor liquid outlet, and the poor urea of discharge is molten
Liquid temperature is 190 DEG C~210 DEG C, and poor urea liquid, into gas-liquid separator, generates after the UTILIZATION OF VESIDUAL HEAT IN of energy-saving heat exchanger
Gas import ammonia mixer, liquid is discharged into urea dissolution/holding vessel by gas-liquid separator liquid outlet, as desalination
Water is used.
In the above-mentioned technical solutions, in S1, urea granules are configured to 50% urea liquid；In S5, hydrolysis reactor
In hydrolysising reacting temperature be 160 DEG C, pressure 1.9Mpa.
The present invention has the advantage that
(1) heating efficiency of the present invention is higher, and energy consumption of the present invention is 0.9MJ/kg NH3, energy consumption of the present invention is than existing skill
Art reduces by 7~10%, and conversion ratio of the present invention is 99%, and yield of the invention improves 5% or more than the prior art, energy of the present invention
Consume lower, ammonia high conversion rate, cost is relatively low；
(2) steam-heating system of the present invention is divided into two strands, and wherein one steam stream is passed through in heating coil and urea liquid
Indirect heat exchange is carried out, the condensate liquid after heat exchange still contains higher temperature, is introduced into urea dissolving tank, for dissolving by heating
Tank promotes the dissolution (urea dissolves about 40 DEG C of required temperature) of urea, improves the utilization rate of energy；Another burst of steam stream is as vapour
It mentions steam directly to spray into hydrolysis of urea reactor by spray head, accelerates NH in urea liquid3The release of gaseous mixture, takes away urea
The NH of the dissolution that hydrolysis generates in the solution3And CO2, while urea liquid is disturbed, is stirred, solution is heated evenly, and makes to urinate
Element hydrolysis is more thorough, and heat transfer efficiency is high, and the waste heat of stripped vapor can also keep the temperature ammonia gas mixture conveyance conduit, prevent
Hui Ning；
(3) waste heat of poor urea liquid is used as the preheating of urea feedstock solution by the present invention, promotes the utilization of waste heat, energy
Energy-efficient effect is played, the poor urea liquid (almost pure water contains certain temperature) after heat exchange utilizes is reused for urea
Dissolution, reduce the use of dissolution demineralized water and the investment of heat to a certain extent.
Detailed description of the invention
Fig. 1 is schematic structural view of the invention.
1- urea dissolution/holding vessel in figure, 1.1- water inlet, 1.2- water outlet, the first connecting pipeline of 1.3-, 1.4- second
Connecting pipeline, 2- circulation conveying pump, 3- energy-saving heat exchanger, 4- hydrolysis reactor, 4.1- hydrolysis reactor liquid outlet, 4.2-
Third connecting pipe, 4.3- hydrolysis reactor water inlet, 5- cooling decompression device, 6- ammonia mixer, 7- dilution air, 8- gas
Liquid/gas separator, 8.1- gas discharge outlet, 8.2- gas-liquid separator liquid outlet, 9- nozzle, the first solenoid electric valve of 10-, 11-
Heating coil, 12- stripped vapor spraying system, 13- dissolve heating tube, the second solenoid electric valve of 14-, 15- third Electromagnetic Control
Valve, 16- waste water treatment system, 17- steam-heating system, 18- DW system demineralized water system, 19- urea system.
Specific embodiment
The performance that the invention will now be described in detail with reference to the accompanying drawings, but they and do not constitute a limitation of the invention, only
It is for example.Keep advantages of the present invention more clear by explanation simultaneously and is readily appreciated that.
Refering to known to attached drawing: urea hydrolysis ammonia producing system, including urea dissolution/holding vessel 1, hydrolysis reactor 4 and steam
Heating system 17, the flow of superheated steam that steam-heating system 17 generates are divided into two strands, one steam stream is passed through by connecting pipeline
In heating coil 11, the heating coil 11 is located in the hydrolysis reactor 4, and another burst of steam stream is passed through by connecting pipeline
Stripped vapor spraying system 12, the stripped vapor spraying system 12 are located at the bottom of the hydrolysis reactor 4, stripped vapor spray
The NH of dissolution can be taken away by penetrating system 123And CO2, play the role of disturbance, stirring is heated evenly solution, moreover it is possible to mixed
Ammonia gas mixture body is kept the temperature, and anti-non-return is solidifying；
11 water outlet of heating coil is connected to by connecting pipeline with dissolution heating tube 13, and described dissolution heating tube 13
In in the urea dissolution/holding vessel 1；In hydrolysis of urea tank after the steam condensation of indirect heating, temperature still with higher,
It is introduced into urea dissolving tank, for dissolving by heating tank, the dissolution of urea is can promote, improves the utilization rate of energy；
1 water outlet 1.2 of urea dissolution/holding vessel is equipped with the first connecting pipeline 1.3 of connection water inlet 1.1, institute
It states and is successively arranged circulation conveying pump 2 and the second solenoid electric valve 14 on the first connecting pipeline 1.3, circulation conveying pump 2 can promote urine
Circulation of the plain solution in pipeline, accelerates course of dissolution, and the urea liquid dissolved delivers into hydrolysis of urea system；
There is hydrolysis reactor water inlet 4.3 to be set to 4 lower end of hydrolysis reactor, is set on the urea dissolution/holding vessel 1
There is the second connecting pipeline 1.4 for being connected to the hydrolysis reactor 4,1.4 both ends of the second connecting pipeline are separately connected 1.2 He of water outlet
Hydrolysis reactor water inlet 4.3；It is successively arranged the circulation conveying on the pipeline and pumps the 2, first solenoid electric valve 10 and energy conservation
Heat exchanger 3, energy-saving heat exchanger are changed as the poor urea liquid in urea liquid preheating device, with the second connecting pipeline 1.4
Heat；
4 lower end of hydrolysis reactor is equipped with hydrolysis reactor liquid outlet 4.1, the hydrolysis reactor liquid discharge
Mouth 4.1 is connected by third connecting pipe 4.2 with gas-liquid separator 8, and the third connecting pipe 4.2 exchanges heat with the energy conservation
Device 3 is connected, and energy-saving heat exchanger exchanges heat as urea liquid preheating device with poor urea liquid；
8 upper end of gas-liquid separator is equipped with gas discharge outlet 8.1, and the gas discharge outlet 8.1 is mixed with the ammonia
Device 6 is connected, lower end is equipped with gas-liquid separator liquid outlet 8.2, the gas-liquid separator liquid outlet 8.2 and the urine
Plain dissolution/holding vessel 1 is connected, and liquid is discharged into urea dissolving tank, uses (urea containing minute quantity) as demineralized water, is reused for urinating
The dissolution of element, reduces the use of dissolution demineralized water and the investment of heat to a certain extent；
4 upper end of hydrolysis reactor is connected to nozzle 9, and the nozzle 9 is passed through ammonia mixer 6；Dilution air 7 passes through
Connecting pipeline is connected with the ammonia mixer 6；The ammonia mixer 6 is equipped with the pipeline towards flue denitrating system.
The connecting pipeline of the gas-liquid separator 8 and the urea dissolution/holding vessel 1 is equipped with third solenoid electric valve
15。
The water inlet 1.1 of the urea dissolution/holding vessel 1 is set to the upper of 1 water outlet 1.2 of urea dissolution/holding vessel
It is square, it is equipped with circulation conveying between inlet and outlet and pumps, circulation conveying pump can promote circulation of the urea liquid in pipeline, add
Fast course of dissolution, the urea liquid dissolved deliver into hydrolysis of urea system.
13 water outlet of dissolution heating tube is connected to by connecting pipeline with waste water treatment system 16.
The connecting pipeline that the steam stream that the steam-heating system 17 generates is passed through heating coil 11 is equipped with cooling decompression
Device 5 is adjusted to meeting demand the temperature and pressure of steam stream.
The hydrolysis of urea method of urea hydrolysis ammonia producing system of the present invention, includes the following steps:
S1: the density in urea system 19 is 1.335kg/m3Urea granules and DW system demineralized water system 18 in demineralized water it is logical
Corresponding entrance is crossed to be added in urea dissolution/holding vessel 1, the urea granules that density is 1.335kg/m3 are configured to 40%~
60% urea liquid；
S2: the heat of urea dissolving tank is passed through molten in urea dissolution/holding vessel 1 by the condensate liquid of hydrolysis reactor coil pipe
Heating tube is solved to provide (control heat-exchange temperature is 40 DEG C), urea is dissolved as the endothermic reaction, and heating can promote the dissolution of urea, molten
Solution heating tube is discharged into waste water treatment system；
S3: circulation conveying pump 2 can promote circulation of the urea liquid in pipeline, accelerate course of dissolution, the urea dissolved
Solution delivers into hydrolysis of urea system；
S4: being provided with energy-saving heat exchanger 3 on transfer pipeline, as urea liquid preheating device, with poor urea liquid into
Urea liquid on second connecting pipeline 1.4 is increased to about 170 DEG C from 40 DEG C by row heat exchange, energy-saving heat exchanger 3；
S5: being provided with steam-heating system in hydrolysis reactor, for providing the heat of hydrolysis of urea, controls hydrolysis
Device temperature is 150 DEG C~170 DEG C, and pressure is 1.8Mpa~2.1Mpa；Steam-heating system herein, exactly hydrolysis reactor
Heating coil provides heat by coil heat exchange because the medium that the inside is walked is exactly steam for hydrolysis；
S6: 4 bottom of hydrolysis reactor is provided with stripped vapor spraying system 12, can take away the NH of dissolution3And CO2, play and disturb
Dynamic, the effect of stirring is heated evenly solution, moreover it is possible to keep the temperature to mixed ammonia gas mixture body, anti-non-return is solidifying；
S7: hydrolysis reactor 4 is discharged by nozzle 9 in the ammonia gas mixture generated in hydrolysis reactor 4, and ammonia gas mixture is logical
Cross nozzle 9 be sent into ammonia mixer 6, pressure of the ammonia gas mixture at nozzle 9 by 1.9Mpa~2.1MPa drop to 0.2Mpa~
0.3Mpa；
S8: air is sent into ammonia mixer 6 by dilution air 7, is 30%~35% by ammonia level in ammonia mixer 6
Ammonia gas mixture be diluted to ammonia level be 5% after, be sent into flue denitrating system；
S9: the poor urea liquid generated after hydrolysis is discharged by outlet, and 190~210 DEG C of poor urea liquid is through energy conservation
After heat exchanger carries out UTILIZATION OF VESIDUAL HEAT IN, into gas-liquid separator 8, the gas of generation imports ammonia mixer pipeline, and liquid is discharged into urine
Plain dissolution/holding vessel 1, as demineralized water with (urea containing minute quantity, the liquid area content is less than 0.5%, NH3It is about
7ppm)。
In S1, urea granules are configured to 50% urea liquid；In S5, the hydrolysising reacting temperature in hydrolysis reactor is
160 DEG C, pressure 1.9Mpa.
Embodiment 1
Hydrolysis of urea prepares the hydrolysis of urea method of ammonia system, includes the following steps:
S1: the density in urea system 19 is 1.335kg/m3Urea granules and DW system demineralized water system 18 in desalination moisture
It is not added in urea dissolution/holding vessel 1 by corresponding entrance, urea granules is configured to 40% urea liquid；
S2: the condensate liquid of hydrolysis reactor coil pipe is passed through the dissolution heating tube 13 in urea dissolution/holding vessel 1, and urea is molten
It is 40 DEG C that urea liquid in solution/holding vessel 1, which passes through dissolution heating tube 13 and condensed heat transfer fluid to temperature, dissolution heating tube water outlet
Into waste water treatment system；
S3: circulation conveying pump 2 promotes circulation of the urea liquid in pipeline, accelerates course of dissolution, and the urea of dissolution is molten
Liquid delivers into hydrolysis of urea system；
S4: the urea liquid on transfer pipeline is increased to 170 DEG C from 40 DEG C by the energy-saving heat exchanger 3 on transfer pipeline；
S5: the hydrolysis in hydrolysis reactor is controlled by steam-heating system, the hydrolysis in hydrolysis reactor
Temperature is 150 DEG C, pressure 1.8Mpa；
S6: the stripped vapor spraying system 12 of 4 bottom of hydrolysis reactor setting takes away ammonia gas mixture；
S7: hydrolysis reactor 4 is discharged by nozzle 9 in the ammonia gas mixture generated in hydrolysis reactor 4, and ammonia gas mixture is logical
It crosses nozzle 9 and is sent into ammonia mixer 6；Pressure of the ammonia gas mixture at nozzle by 1.9Mpa~2.1MPa drop to 0.2Mpa~
0.3Mpa；
S8: air is sent into ammonia mixer 6 by dilution air 7, is 30%~35% by ammonia level in ammonia mixer 6
Ammonia gas mixture be diluted to ammonia level be 5% after, be sent into flue denitrating system；
S9: the poor urea liquid generated after hydrolysis is discharged by hydrolysis reactor liquid outlet 4.1, the poor urea of discharge
Solution temperature is 190 DEG C~210 DEG C, and poor urea liquid is after the UTILIZATION OF VESIDUAL HEAT IN of energy-saving heat exchanger 3, into gas-liquid separator 8,
The gas of generation imports ammonia mixer 6, and liquid is discharged into urea dissolution/holding vessel by gas-liquid separator liquid outlet 8.2
1, it is used as demineralized water.
Conclusion: energy consumption 0.9MJ/kgNH3(ammonia), ammonia (NH3) conversion ratio be 99.0%.
Embodiment 2
In S1, urea granules are configured to 50% urea liquid；Hydrolysis temperature in S5, in hydrolysis reactor
Degree is 160 DEG C, pressure 1.9Mpa；Other methods step is same
Embodiment 1.
Conclusion: energy consumption 0.9MJ/kgNH3, the conversion ratio of ammonia is 99.6%.
Embodiment 3
In S1, urea granules are configured to 60% urea liquid；Hydrolysis temperature in S5, in hydrolysis reactor
Degree is 170 DEG C, pressure 2.1Mpa；Other methods step is same
Embodiment 1.
Conclusion: energy consumption 0.9MJ/kgNH3, the conversion ratio of ammonia is 99.5%.
Other unaccounted parts belong to the prior art.
Claims (7)
1. urea hydrolysis ammonia producing system, it is characterised in that: including urea dissolution/holding vessel (1), hydrolysis reactor (4) and steam
Heating system (17), the steam stream that steam-heating system (17) generates are divided into two strands, one steam stream is passed through by connecting pipeline
In heating coil (11), the heating coil (11) is located in the hydrolysis reactor (4), and another burst of steam stream passes through communicating pipe
Road is passed through stripped vapor spraying system (12), and the stripped vapor spraying system (12) is located at the bottom of the hydrolysis reactor (4)
Portion；
Heating coil (11) water outlet is connected to by connecting pipeline with dissolution heating tube (13), the dissolution heating tube (13)
In the urea dissolution/holding vessel (1)；
The urea dissolution/holding vessel (1) water outlet (1.2) is equipped with the first connecting pipeline of connection water inlet (1.1)
(1.3), circulation conveying pump (2) and the second solenoid electric valve (14) are successively arranged on first connecting pipeline (1.3)；
There are hydrolysis reactor water inlet (4.3) on the hydrolysis reactor (4) lower end, the urea dissolution/holding vessel (1)
Equipped with the second connecting pipeline (1.4) for being connected to the hydrolysis reactor (4)；It is successively arranged on second connecting pipeline (1.4)
The circulation conveying pump (2), the first solenoid electric valve (10) and energy-saving heat exchanger (3)；
Hydrolysis reactor (4) lower end is equipped with hydrolysis reactor liquid outlet (4.1), the hydrolysis reactor liquid discharge
Mouthful (4.1) are connected by third connecting pipe (4.2) with gas-liquid separator (8), the third connecting pipe (4.2) with it is described
Energy-saving heat exchanger (3) is connected；
Gas-liquid separator (8) upper end is equipped with gas discharge outlet (8.1), and the gas discharge outlet (8.1) and the ammonia are mixed
Clutch (6) is connected, lower end is equipped with gas-liquid separator liquid outlet (8.2), the gas-liquid separator liquid outlet (8.2)
It is connected with the urea dissolution/holding vessel (1)；
Hydrolysis reactor (4) upper end is connected to nozzle (9), and the nozzle (9) is passed through ammonia mixer (6)；Dilution air
(7) it is connected by connecting pipeline with the ammonia mixer (6)；The ammonia mixer (6), which is equipped with, leads to flue denitration
The pipeline of system.
2. urea hydrolysis ammonia producing system according to claim 1, it is characterised in that: the gas-liquid separator (8) with it is described
Urea dissolution/holding vessel (1) connecting pipeline is equipped with third solenoid electric valve (15).
3. urea hydrolysis ammonia producing system according to claim 1 or 2, it is characterised in that: the urea dissolution/holding vessel
(1) water inlet (1.1) is set to the top of water outlet (1.2).
4. urea hydrolysis ammonia producing system according to claim 3, it is characterised in that: dissolution heating tube (13) water outlet
It is connected to by connecting pipeline with waste water treatment system (16).
5. urea hydrolysis ammonia producing system according to claim 4, it is characterised in that: the steam-heating system (17) generates
Steam stream be passed through heating coil (11) connecting pipeline be equipped with cooling decompression device (5).
6. urea hydrolysis ammonia producing system described in any claim hydrolyzes ammonia method processed, feature in -5 according to claim 1
It is: includes the following steps:
S1: the urea granules in urea system (19) are added to the demineralized water in DW system demineralized water system (18) by corresponding entrance
In urea dissolution/holding vessel (1), urea granules are configured to 40%~60% urea liquid；
S2: the condensate liquid of heating coil is passed through the dissolution heating tube in urea dissolution/holding vessel (1) in hydrolysis reactor (4)
(13), the urea liquid in urea dissolution/holding vessel (1) is 40 by dissolution heating tube (13) and condensed heat transfer fluid to temperature
DEG C, dissolution heating tube (13) is discharged into waste water treatment system；
S3: circulation conveying pumps (2) and promotes circulation of the urea liquid in pipeline, accelerates course of dissolution, by the urea liquid of dissolution
Deliver into hydrolysis of urea system；
S4: the urea liquid on the second connecting pipeline (1.4) is increased to by the energy-saving heat exchanger (3) on transfer pipeline from 40 DEG C
160 DEG C~180 DEG C；
S5: by the hydrolysis in steam-heating system (17) control hydrolysis reactor (4), the hydrolysis in hydrolysis reactor is anti-
Answering temperature is 150 DEG C~170 DEG C, and pressure is 1.8Mpa~2.1Mpa；
S6: the stripped vapor spraying system (12) of hydrolysis reactor (4) bottom setting takes away ammonia gas mixture；
S7: the ammonia gas mixture generated in hydrolysis reactor (4) passes through nozzle (9) discharge hydrolysis reactor (4), ammonia gas mixture
Ammonia mixer (6) are sent by nozzle (9)；
S8: dilution air (7) by air be sent into ammonia mixer (6), by ammonia level in ammonia mixer (6) be 30%~
35% ammonia gas mixture be diluted to ammonia level be 5% after, be sent into flue denitrating system；
S9: the poor urea liquid generated after hydrolysis is discharged by hydrolysis reactor liquid outlet (4.1), and the poor urea of discharge is molten
Liquid temperature is 190 DEG C~210 DEG C, and poor urea liquid is after the UTILIZATION OF VESIDUAL HEAT IN of energy-saving heat exchanger (3), into gas-liquid separator
(8), the gas of generation imports ammonia mixer (6), and to be discharged into urea molten by gas-liquid separator liquid outlet (8.2) for liquid
Solution/holding vessel (1) is used as demineralized water.
7. urea hydrolysis ammonia producing system according to claim 6 hydrolyzes ammonia method processed, it is characterised in that: in S1, by urea
Particle is configured to 50% urea liquid；In S5, the hydrolysising reacting temperature in hydrolysis reactor (4) is 160 DEG C, and pressure is
1.9Mpa。
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| CN110963506A (en) * | 2019-12-26 | 2020-04-07 | 内蒙古电力(集团)有限责任公司内蒙古电力科学研究院分公司 | Urea ammonia production system with injection steam as auxiliary heat source |
| CN111036076A (en) * | 2019-12-26 | 2020-04-21 | 内蒙古电力(集团)有限责任公司内蒙古电力科学研究院分公司 | Urea hydrolysis ammonia supply system with injection steam as heat source |
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| CN112691561A (en) * | 2020-12-22 | 2021-04-23 | 青岛诺瑞尔节能环保科技有限公司 | Gas-liquid mixer for denitration and use method thereof |
| CN112499649A (en) * | 2020-12-24 | 2021-03-16 | 昆山市三维换热器有限公司 | Urea hydrolysis ammonia dehydration system and method thereof |
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