CN107159081B - Urea hydrolysis ammonia production process adopting urea rising film type self-circulation hydrolysis reactor - Google Patents
Urea hydrolysis ammonia production process adopting urea rising film type self-circulation hydrolysis reactor Download PDFInfo
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2475—Membrane reactors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J14/00—Chemical processes in general for reacting liquids with liquids; Apparatus specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
- B01J2219/00081—Tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
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- 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
Abstract
A climbing film reactor and a method for preparing ammonia by urea hydrolysis. The reactor consists of a preheater and a rising film type self-circulation reactor. The urea solution is heated to a temperature close to the temperature required for the reaction by a preheater. Heating and hydrolyzing the urea in a rising film type self-circulation reactor to generate ammonia gas and carbon dioxide. The preheater may employ a plate or shell and tube heat exchanger. In the rising film type self-circulation reactor, the urea solution is in a tube side, and the steam is condensed in a shell side, so that the heat exchange efficiency is improved, and the required heat exchange area and the manufacturing cost are reduced. The amount of the solution held in the reactor is low, the yield of the ammonia gas can be controlled by adjusting the flow of the steam and the flow of the urea solution, the response time to the fluctuation change of the ammonia gas is short, and the phenomenon of insufficient ammonia supply or ammonia escape caused by the fluctuation of the flue gas of the boiler is avoided. The preheater and the reactor are designed separately, and the film-raising self-circulation reactor is of a vertical structure. Therefore, the whole floor area of the equipment is small, and the civil engineering installation cost of the equipment is reduced.
Description
Technical field
The present invention relates to a kind of for the denitrating flue gas method of urea hydro-thermal ammonia, is more specifically exactly to invent one kind to adopt
Membrane type self-loopa hydrolysis reactor, which is risen, with urea carries out hydrolysis of urea ammonia method.
Background technique
Selective catalytic reduction (selective catalytic reduction) denitrating technique is current coal-burning power plant
Main denitrating technique, principle be under the action of certain temperature and catalyst, reducing agent selectively the NOx in flue gas also
It originally was free of contamination N2 and water.The reducing agent of industrial application is mainly ammonia either urea at present, wherein using ammonia as reduction
Agent needs to evaporate supply system using ammonia, i.e., liquefied ammonia is first evaporated to ammonia, then by ammonia surge tank, then again with sky
Gas (using dilution air convey) mix in a mixer, then enter back into ammonia-spraying grid, finally enter back into catalytic reactor into
Row reaction.Since liquefied ammonia needs the problems such as fire-proof and explosion-proof in transport, storage.In the area produced partially away from liquefied ammonia, or in electricity
Ammonia needed for factory residential neighborhood mainly uses process for producing ammonia from urea to provide denitration as safety factor.
Process for producing ammonia from urea includes hydrolysis of urea Ammonia Process and urea pyrolysis Ammonia Process.Wherein hydrolysis of urea ammonia work
Skill can use the reasons such as secondary steam since reaction temperature is low, home-made equipment rate is higher, so that the cost of hydrolysis ammonia processed is low
In urea pyrolysis technique, therefore gradually start to promote in practical engineering applications.Hydrolysis of urea reaction is urea production mistake
The back reaction of journey, reaction 2 steps it is considered that be made of:
NH2CONH2+H2O=NH2COONH4-15.5 kJ/mol (1)
NH2COONH4=2NH3+CO2+177 kJ/mol (2)
Step 1 reaction is that urea and water generate amino ammonium formate and is intended to, which is micro- exothermic reaction, and reaction process is very slow
Slowly；Step 2 reaction is strong endothermic reaction, and carbamic acid amine, which decomposes rapidly, generates ammonia and CO2, reaction process is very fast.It is right
It can accelerate the progress of reaction rate in the presence of the urea liquid of water surplus, excessive water.In the case where there is excessive water participation,
The total chemical equation of hydrolysis of urea are as follows:
NH2CONH2+xH20=2NH3+CO2+ (x 1) H20+161.5 k7/mol (3)
Urea hydrolysis ammonia producing system includes urea storage, discharging feeding device, and urea liquid prepares and storage facilities, urea
The conveying of solution and recycle unit, the hydrolysis reactor of urea liquid.Wherein hydrolysis of urea reactor is hydrolysis of urea ammonia
Core equipment.Currently, part power plant is applied at home for the hydrolysis of urea reaction process and device of certain domestic enterprise development.Its
Structure and technical characters are as follows:
1) ammonia tank reactor processed is hydrolyzed using urea liquid, is mainly existed by autoclave cylindrical structure reaction kettle and setting
U-shaped heat exchange coil inside horizontal long cartridge type reaction kettle and the product gas being arranged on horizontal long cartridge type reaction kettle outer wall go out
Mouth pipe and urea liquid are injected into material mouth composition.
2) reactor is completely soaked in by heat transfer urea liquid using U-shaped heat exchange coil, internal after Cold Side Liquid is heated
From bottom to top carry out self-loopa.
3) heating steam is heated urea liquid shell side in tube side.Tube side is completely submerged in reaction solution compared with shell side.
4) it is designed using skid, reactor and associated pipe thermal control device modular integratedization is designed.
Its major advantage is skid, modularized design.But there are the following problems:
1) tube side is heating steam, and steam is condensed in tube side inner wall in heat transfer process and forms liquid film, though there is high velocity vapor
Purge it is thinning, but still influence heat exchange efficiency.Especially liquid liquid heat exchange efficiency is likely to form more in the increasing of tube side end condensing capacity
It is low.
2) since reaction solution is in shell side, main heat exchange reaction occurs in U-tube outer wall, and reaction solution is decomposed to form on the outer wall
Micro-bubble is diffused into reaction solution and escapes.And the formation of micro-bubble declines very compared with liquid/solid (U tube wall) heat exchange efficiency
It is more.
3) since reaction solution is in shell side, the reaction solution ownership of reactor is big.
Although 4) be provided with hydraulic barrier in shell side, compared with reaction solution is in tube side, reaction flow velocity is too low on the outside of U pipe
It is unfavorable for equipment heat exchange to remain in a standstill.
5) excessive reactor volume improves the cost of equipment, while the integral heat insulation for being unfavorable for equipment increases equipment
Energy consumption.
Based on problem 1), 2), 4) the reason of, the reactor, heat exchange efficiency is low, heat exchange needed for completing identical heat exchange amount
Area increases, and has correspondinglyd increase the volume of reactor.Due to problem 3) and excessive reactor volume make reaction solution in reactor
The ownership of urea liquid is big, and under the conditions of SCR load variations, the response time that reaction generates ammonia is too long.Due to reactor
Using horizontal long cartridge type reaction kettle, volume is excessive, and reaction solution ownership is big, and reaction solution is heated to required reaction temperature when starting
Overlong time, while more stringent requirements are proposed for occupied area to equipment and equipment load.The water of its hydrazine yield 126kg/h processed
Solution its occupied area of reactor is 7mX2.5m.
Since reactor in SCR load variations to due to causing the response time of ammonia flow fluctuation too long, equipment is being opened
The reasons such as starting overlong time, cause ammonia to be escaped or since ammonia amount deficiency leads to nitrogen oxides in effluent row not up to standard when dynamic
It puts.
Therefore, it is necessary to research and develop, a kind of heat exchange efficiency is high, and occupied area is small, and the response time is short, starting time shorter urine
Plain hydrolysis reactor.
Summary of the invention
The object of the present invention is to provide a kind of heat exchange efficiency height, occupied area is small, the response time is short, the starting time is shorter
The method and technique of hydrolysis of urea ammonia.
To achieve the above object, the present invention is with the following method: a kind of to rise membrane type self-loopa hydrolysis reactor using urea
Hydrolysis of urea Ammonia Process, it is characterised in that: reactor vertically vertical installation, using tube shell type structure, urea liquid is in pipe
Journey, water vapour is in shell side, into reactor, is decomposed thermally to form ammonia and carbon dioxide in pipe side, reacted on the gas of generation
It rises to reactor head and is discharged through steam-water separator.Tube side of urea liquid under the action of air-flow in reactor is with shaped liquid film
Reactor is raised under state holds liquid layer；2) a urea cycle connecting tube, urea are equipped between the top of reactor and bottom
Solution maintains certain urea liquid liquid level after reaching reactor top, on top, and the urea liquid carried secretly up is by urine
Element is connected by circulation pipe and is back to reactor bottom, since the density of liquid is greater than the density of gas-liquid mixture, in inside reactor
Form the circulation of urea liquid；3) urea liquid from reactor bottom urea cycle connecting tube horizontal segment enter, urea liquid into
Mouth occurs in the form of jet pipe in urea cycle connecting tube.Promote inside reactor using the flow at high speed of import urea liquid
Solution circulation；It 4) is one or more in shell side heating steam inlet, it can be according on reactor for multiple steam inlets
In under (or up and down) layered arrangement, every layer of steam inlet should be evenly distributed with；5) area of its heat exchanger tube should be according to the equipment of reactor
Power output (yield of ammonia) determines, and has 50% design capacity.For the flowing velocity for accelerating urea liquid in managing, equipment entirety
Draw ratio be not less than 5, the draw ratio of heat exchanger tube is not less than 100, generally 300.The overall diameter of heat exchanger tube is not more than 15mm.Pipe
Interior gas flow rate is not less than 15m/s, generally 30m/s；6) mass concentration of the urea liquid of its import is 40%~50%, specific gravity
1.13~1.15, pH value 7~10；7) there is demister on the top of reactor, demister is screen type or other suitable forms, is removed
Day with fog should be arranged two layers, and removal reaction generates the urea liquid of ammonia carbon dioxide entrained with；8) reactor shell side bottom is equipped with
Drain port, condensed water drain into drain recovery water tank (sharing with the recycling condensed water of preheater) through drain valve by drain port.It dredges
The recycle-water of water recycling bins can be used for the dissolution or other purposes of urea；9) material of the shell side of reactor can use 304
Stainless steel or carbon steel, heat exchanger tube, the upper and lower end socket of reactor, demister etc. and ammonia and urea contact portion should using 304 or
316L stainless steel；10) blowdown valve should be equipped in the lower part of reactor, the shell side top of reactor be equipped with safety valve and temperature,
Device for pressure measurement；11) reactor outlet has heating coil, and the gas that reactor is discharged is higher than their dew point temperature
Degree.It is general to be not less than 150 DEG C.
The above-mentioned signified hydrolysis of urea Ammonia Process that membrane type self-loopa hydrolysis reactor is risen using urea, feature is such as
Under: 1) in urea liquid warm-up phase by the flow or switch of control heating vapor, control urea liquid goes out in preheater
The temperature of mouth maintains 130 DEG C, and outlet pressure is not less than 0.55MPa.In the first stage by hydrolysis of urea reaction controlling, avoid by
The heat transfer effect of ammonia and effect of carbon dioxide preheater is generated in preheater premature hydrolysis in urea；2) in hydrolysis ammonia rank
Section controls the ammonia production quantity of reactor by the flow of control heating vapor and urea liquid.To meet under different operating conditions
The ammonia usage of denitrating flue gas.Reaction temperature is controlled at 145 DEG C~165 DEG C, reaction pressure is in 0.55~0.70MPa；
The above-mentioned signified hydrolysis of urea Ammonia Process that membrane type self-loopa hydrolysis reactor is risen using urea, comprising: urea
Storage and transportation, urea dissolution, urea liquid conveying, urea liquid pre-heating system, urea hydrolysis ammonia producing system and drain recovery water tank
And the ancillary equipments such as drainage pump composition.It should be noted that following problems: 1)
The vapour source that urea depth hydrolysis' ammonia system uses is that heating steam is pressed in power plant, about 3.5 MPa of vapour source pressure, temperature
420 DEG C two of degree obtains 0.5~0.8 MPa of pressure by reducing-and-cooling plant, and the steam that 150 DEG C~170 DEG C of temperature is for hydrolysis
System uses；2) the ammonia pipeline connecting with hydrolysis reactor should reinforce heat tracing and heat preservation, be that temperature is not less than gaseous mixture in pipeline
The dew-point temperature of body；3) under the conditions of possible, ammonia absorption system is provided in hydrolysis of urea region, for ammonia under accident condition
The absorption of gas.The system is mainly made of ammonia tourie, connecting pipe and spray waterpipe.Hydrolysis of urea reactor, ammonia are slow
It rushes tank safety door discharge tube and is connected to ammonia tourie.There is the in line ammonia tourie of pipeline in hydrolyzer outlet, abnormal when occurring
When, ammonia is discharged into ammonia tourie, and when temperature reaches 40 DEG C in tourie, spray is opened in starting, and a large amount of fire waters, which spray, to be absorbed
Ammonia.Ammonia-containing water is discharged into effluent pit by the overflow pipe of ammonia tourie；4) should reinforce in the conveyance conduit of urea
Heat preservation and heat tracing are the temperature of urea liquid not less than 40 DEG C, prevent from leading to line clogging due to the lower urea crystals of temperature.
Wherein, the above-mentioned signified urea liquid preheating system for rising membrane type self-loopa hydrolysis reactor for urea is main
Formed including urea liquid preheater and associated pipe, it is characterised in that: 1) pre-heater can using shell-and-tube heat exchanger or
Plate heat exchanger flows shell-and-tube heat exchanger urea liquid in pipe side, and water vapour is in shell-side condensation, for plate heat exchanger
It is steam that then side, which is the urea liquid other side,；2) condensed water of heat exchanger is arranged by the drain port of preheater bottom through drain valve
It (is shared to drain recovery water tank with liter recycling condensed water of film self-loopa hydrolysis of urea reactor).The recycling of drain recovery water tank
Water can be used for the dissolution or other purposes of urea.3) heat exchange area of preheater should meet urea liquid and be heated to connecing from room temperature
150% of heat exchange area needed for proximal response temperature (130 DEG C), the temperature for heating steam is 135 DEG C~140 DEG C.
Detailed description of the invention
The present invention will be further described in detail with reference to the accompanying drawing.
Fig. 1 is the hydrolysis of urea Ammonia Process flow diagram that membrane type self-loopa hydrolysis reactor is risen using urea；
Fig. 2 is the structural schematic diagram that urea rises membrane type self-loopa hydrolysis reactor；
1 lower head, 2 liters of membrane heat exchangers, 3 demisters, 4 upper covers, 5 urea cycle connecting tubes, 6 urea liquids recycle into
Mouth, 7 sewage draining exits, 8 heating steam inlets (one or more), 9 drain ports, 10 thermometer bosses, 11 pressure gauge connections, 12 shell sides
Relief valve connection.13 urea liquid overflow ports, 14 liquidometer mouths, 15 level-one demister layers, 16 second level demister layers, 17 heat exchange
Steam pipe coil, 18 ammonias and carbon dioxide outlet, 19 pressure gauge connections, 20 reactor relief valve connections, 21 thermometer bosses.
Hydrolysis of urea Ammonia Process is made of following equipment and associated pump valve pipeline instrument, and specific equipment is as follows: A1 urine
Plain bucket elevator, A2 urea warehouse, A3 urea centre warehouse, A4 urea dissolving tank, A5 urea liquid storage tank, the preheating of A6 urea liquid
Device, A7 rise membrane type self-loopa hydrolysis reactor, A8 ammonia surge tank, A9 drain recovery water tank, A10 ammonia absorption system.
Pre-heater can use shell-and-tube heat exchanger or plate heat exchanger, for shell-and-tube heat exchanger urea liquid in pipe
Side flowing, for water vapour in shell-side condensation, it is that steam urea rises membrane type that for plate heat exchanger, then side, which is the urea liquid other side,
Self-loopa hydrolysis reactor is mainly by 1 lower head, 2 liters of membrane heat exchangers, 3 demisters, 4 upper covers, 5 urea cycle connecting tube groups
At.6 urea liquids, which are equipped with, in lower head recycles import, 7 sewage draining exits.Liter film heat exchanger be equipped with 8 heating steam inlets (one or
It is multiple), 9 drain ports, 10 thermometer bosses, 11 pressure gauge connections, 12 relief valve connections.It is molten that 13 urea are equipped in demister lower part
Hydrorrhea head piece and 14 liquidometer mouths, demister top include 15 level-one demisters, 16 second level demisters, 17 heat exchange steam discs
Pipe.Upper cover is equipped with 18 ammonias and carbon dioxide outlet, 19 pressure gauge connections, 20 relief valve connections.In urea liquid circulation pipe
Equipped with 21 thermometer bosses.
Specific embodiment
Embodiment is shown in Figure 1, and this urea rises membrane type self-loopa hydrolysis reactor by urea liquid preheater and liter
Membrane type self-loopa hydrolysis reactor two parts composition.Urea is defeated through urea bucket elevator after being transported to hydrolysis of urea ammonia place outside
Send to urea warehouse and urea dissolving tank dropped down by gravity through warehouse among urea (metering with), urea dissolving tank it is agitated and
Heating is dissolved into 45%~55% urea liquid in demineralized water, is pumped to urea liquid storage tank through urea mixing pump, urea is molten
The urea liquid of liquid storage tank is delivered to urea liquid preheater through urea delivery pump, molten in the urea of urea liquid preheater tube side
Liquid rises a membrane type self-loopa hydrolysis reactor to entering after 135 DEG C by Secondary-steam heating, urea liquid reactor tube side
In uphill process, urea liquid absorbs heat in tube wall and hydrolysis generation ammonia and carbon dioxide occurs, and escapes from tube wall
Gas rapid increase is thinned the thickness of liquid film of heat exchange tube wall urea liquid, has driven the climbing speed of urea liquid, has improved
The heat exchange efficiency of reactor, when the top of urea liquid to reactor due to the urea refluxing opening of reactor and tube side and centainly
Distance holds liquid layer what reactor top formd certain altitude, molten due to holding urea of the presence of liquid layer on reactor top
Liquid is back to reactor tube-side inlet under the effect of gravity, mixes with the urea liquid for entering reactor and re-starts hydrolysis instead
It answers.Enter ammonia surge tank use after reacting the demister removal urea liquid of the ammonia, the reacted device top of carbon dioxide that generate
It is reacted in boiler of power plant denitrating flue gas.The steam condensed in urea preheater and hydrolysis of urea reactor is arranged through drain valve is unified
Put the dissolution to drain recovery water tank for urea or other process waters.It is equipped with ammonia absorption system in urea ammonia region,
Absorption for ammonia under accident condition.The system is mainly made of ammonia tourie, connecting pipe and spray waterpipe.Hydrolysis
Device, ammonia surge tank safety door discharge tube are connected to ammonia tourie.There is the in line ammonia tourie of pipeline in hydrolyzer outlet, when
When occurring abnormal, ammonia is discharged into ammonia tourie, and when temperature reaches 40 DEG C in tourie, spray, a large amount of fire waters are opened in starting
It sprays and absorbs ammonia.Ammonia-containing water is discharged into effluent pit by the overflow pipe of ammonia tourie.
Claims (7)
1. a kind of hydrolysis of urea Ammonia Process for rising membrane type self-loopa hydrolysis reactor using urea, it is characterised in that: urea water
Solution Ammonia Process include urea storage and transportation, urea dissolution, urea liquid conveying, urea pre-heating system, urea hydrolysis ammonia producing system, with
And drain recovery water tank and drainage pump；
Urea hydrolysis ammonia producing system includes that urea rises membrane type self-loopa hydrolysis reactor, reactor vertically vertical installation, using pipe
Shell type structure, urea liquid is in tube side, and for water vapour in shell side, urea liquid enters reactor close under the conditions of decomposition temperature,
Pipe side is decomposed thermally to form ammonia and carbon dioxide, and the gas for reacting generation rises to reactor head and arranges through steam-water separator
Out；What urea liquid was raised to reactor under the action of air-flow in the case where the tube side of reactor is with liquid film state holds liquid layer；
Between the top and bottom of reactor be equipped with a urea cycle connecting tube, urea liquid after reaching reactor top,
Certain urea liquid liquid level is maintained on top, the urea liquid carried secretly up is back to reactor by urea cycle connecting tube
Bottom forms the circulation of urea liquid in inside reactor since the density of liquid is greater than the density of gas-liquid mixture；Urea is molten
Liquid enters from reactor bottom urea cycle connecting tube horizontal segment, and urea liquid import is in urea cycle connecting tube with jet pipe
Form occurs；The solution of inside reactor is promoted to recycle using the flow at high speed of import urea liquid.
2. the hydrolysis of urea Ammonia Process according to claim 1 that membrane type self-loopa hydrolysis reactor is risen using urea,
Be characterized in that: being one to multiple in shell side heating steam inlet, for multiple steam inlets, should according to reactor upper, middle and lower or
Upper and lower layered arrangement, every layer of steam inlet should be evenly distributed with；The area of its heat exchanger tube should contribute according to the equipment of reactor, i.e. ammonia
Yield determines, and has 50% design capacity;To accelerate to manage the flowing velocity of interior urea liquid, the draw ratio of equipment entirety is not small
In 5, the draw ratio L/D of heat exchanger tube is 300；The overall diameter of heat exchanger tube is 15mm；Gas flow rate is 30m/s in managing.
3. the hydrolysis of urea Ammonia Process according to claim 1 that membrane type self-loopa hydrolysis reactor is risen using urea,
Be characterized in that: the mass concentration of its urea liquid is 40%~50%, specific gravity 1.13~1.15, pH value 7~10.
4. the hydrolysis of urea Ammonia Process according to claim 1 that membrane type self-loopa hydrolysis reactor is risen using urea,
It is characterized in that: controlling the ammonia production quantity of reactor using the flow of the steam flow and urea liquid that control hydrolysis reactor；
To meet the ammonia usage of denitrating flue gas under different operating conditions, reaction temperature is controlled at 145 DEG C~165 DEG C, reaction pressure is 0.55
~0.70MPa；The vapour source that urea depth hydrolysis' ammonia system uses is that heating steam is pressed in power plant, vapour source pressure 3.5MPa,
420 DEG C of temperature, 0.5~0.8 MPa of pressure, the steam that 150 DEG C~170 DEG C of temperature, for hydrolysis are obtained by reducing-and-cooling plant
System uses.
5. the hydrolysis of urea Ammonia Process according to claim 1 that membrane type self-loopa hydrolysis reactor is risen using urea,
Be characterized in that: the urea pre-heating system includes preheater, and preheater uses shell-and-tube heat exchanger or plate heat exchanger, for pipe
Shell heat exchanger, urea liquid are flowed in pipe side, and water vapour is in shell-side condensation, and for plate heat exchanger, then side is urea liquid
The other side is steam；The heat exchange area of preheater should meet urea liquid and be heated to from room temperature close to needed for 130 DEG C of reaction temperature
Heat exchange area 150%, heat steam temperature be 135 DEG C~140 DEG C.
6. the hydrolysis of urea Ammonia Process according to claim 5 that membrane type self-loopa hydrolysis reactor is risen using urea,
Be characterized in that: the condensed water of preheater drains into drain recovery water tank through drain valve by the drain port of preheater bottom, i.e., with urine
The recycling condensed water that element rises membrane type self-loopa hydrolysis reactor shares；The recycle-water of drain recovery water tank for urea dissolution or
Other purposes.
7. the hydrolysis of urea Ammonia Process according to claim 5 that membrane type self-loopa hydrolysis reactor is risen using urea,
Be characterized in that: for shell-and-tube heat exchanger, heat exchanger tube material is 316L or 304 stainless steels, and shell side material is contacted with steam
Part uses 304 stainless steels or carbon steel；316L or 304 stainless steels are used for its material of plate heat exchanger.
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| CN107840353A (en) * | 2017-12-18 | 2018-03-27 | 江苏中立环保科技有限公司 | Hydrolysis of urea reactor |
| EP3569305A1 (en) * | 2018-05-16 | 2019-11-20 | Yara International ASA | High pressure strippers for use in urea plants |
| CN110422860A (en) * | 2019-07-16 | 2019-11-08 | 中国华电科工集团有限公司 | A kind of hydrolysis of urea ammonia reaction unit |
| CN111215010A (en) * | 2020-02-27 | 2020-06-02 | 东方电气集团东方锅炉股份有限公司 | Urea hydrolysis reactor utilizing hydrophobic waste heat and urea hydrolysis method thereof |
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