CN103482649B - Urea solution hydrolysis reactor - Google Patents
Urea solution hydrolysis reactor Download PDFInfo
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- CN103482649B CN103482649B CN201310400325.4A CN201310400325A CN103482649B CN 103482649 B CN103482649 B CN 103482649B CN 201310400325 A CN201310400325 A CN 201310400325A CN 103482649 B CN103482649 B CN 103482649B
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Abstract
The invention aims to provide a urea solution hydrolysis reactor which can receive a urea supersaturated solution as an incoming solution to reduce the steam content of an outlet of the reactor, so as to save energy and the consumption of desalted water. The urea solution hydrolysis reactor comprises a reaction kettle of which the bottom part is respectively provided with a urea solution inlet and a reaction liquid outlet, and a heating device and a steam stripping device, wherein the heating device and the steam stripping device are arranged sequentially along the urea flowing direction in the reaction kettle; a reaction gas phase product outlet is formed in the top part of the reaction kettle; the steam stripping device comprises a steam stripping steam inlet communicated to the bottom part of the reaction kettle; one end, extending into the reaction kettle, of the steam stripping steam inlet is connected with a steam stripping steam distributor. By using the steam stripping device, the steam input into the reaction kettle by the steam stripping device is enabled to directly contact the urea solution, in this way, not only is the hydrolysis of the urea solution accelerated, but also the ammonia gas generated in a liquid phase can be accelerated to diffuse continuously into a gas phase and to be output from the reaction gas phase product outlet.
Description
Technical field
The invention belongs to hydrolysis of urea ammonia equipment technical field in flue gas denitrification system, be specifically related to a kind of urea soln hydrolysis reactor.
Background technology
The coal burning of coal-fired power plant is along with a large amount of oxynitride (NO
x) discharge, air is polluted.Usually take to add equipment for denitrifying flue gas at boiler tail, utilize selective catalytic reduction (SCR) to remove NO in flue gas
x, be translated into nontoxic nitrogen (N
2) and water (H
2thus reach emission request O).Denitrification reducing agent ammonia (NH required in selective catalytic reduction
3) usually there are three kinds of supply forms: liquefied ammonia, ammoniacal liquor and urea.Wherein, liquefied ammonia and ammoniacal liquor belong to hazardous chemical.There are strict legal provisions in country relating in the storage of liquefied ammonia and ammoniacal liquor, use and transportation.And industrial urea is white crystals body particle, do not belong to hazardous chemical category, be convenient to store and transport, potential safety hazard can not be caused because leaking, therefore consider from safety and economy angle, urea ammonia is subject to people's favor gradually, by the supply adopting the urea soln hydrolysis method of one of urea ammonia method to realize ammonia.
In existing urea soln hydrolysis reactor, when urea soln injects, consider the solubleness of urea and the security of course of conveying under normal temperature, the urea soln of to be massfraction the be 40%-60% all adopted; According to the chemical equation of hydrolysis of urea
suppose urea solution mass concentration 50%, calculate according to the stoichiometric ratio of hydrolysis of urea reaction, only have the water of solution weight 15% to participate in chemical reaction, all the other water accounting for urea soln weight 35% do not participate in hydrolysis reaction.This excessive water of 35%, after heat absorption vaporization, leaves reactor with reaction product, causes the waste of energy and the desalination water yield.Suppose urea solution mass concentration 60%, calculate according to the stoichiometric ratio of hydrolysis of urea reaction, only have the water of solution weight 18% to participate in chemical reaction, all the other water accounting for urea soln weight 22% do not participate in hydrolysis reaction.
If urea and water are measured than configuring urea soln according to hydrolysis reaction, then the mass concentration of urea soln needs to reach 77%, the urea soln of this concentration must be the supersaturated solution of urea, therefore the supersaturated solution of urea is carried out liquid as hydrolysis reactor, greatly will reduce the content of reactor outlet water vapor, but existing reactor all cannot meet the processing requirement accepting urea supersaturated solution, wastage of material is serious, and power consumption is larger.
Summary of the invention
The object of the invention is to provide a kind of urea soln hydrolysis reactor, can accept urea supersaturated solution as carrying out liquid, reduces reactor outlet vapour content, thus saves energy and desalination water consumption.
The present invention is achieved through the following technical solutions:
A kind of urea soln hydrolysis reactor, comprises the reactor that bottom arranges urea soln opening for feed and reaction solution outlet respectively, and is arranged on the heating unit and stripper plant that set gradually along urea flow direction in reactor; Described reactor top arranges reaction gas phase product exit; Described stripper plant comprises the stripped vapor import being communicated with and being arranged on bottom reactor, and one end that reactor is stretched in stripped vapor import connects stripped vapor divider.
Preferably, described stripper plant also comprises the dividing plate be arranged on above stripped vapor divider, and is arranged on feed liquor weir plate and the fluid weir plate of divider both sides; Dividing plate upper end open forms gas stream and opens one's mouth, and lower ending opening forms liquid stream and opens one's mouth; Feed liquor weir plate is arranged on the updrift side of dividing plate, and upper end open forms liquid inflow port; Fluid weir plate is arranged on the downstream direction of dividing plate, and upper end open forms overflow mouth; Forming reactions stripping zone between feed liquor weir plate and fluid weir plate.
Preferably, described urea soln opening for feed is communicated with urea soln supply line by a feed end of liquid mixing box; Another feed end of liquid mixing box and reaction solution outlet.
Further, described liquid mixing box is also provided with for reaction solution being added the recycle pump of pressing and being injected in liquid mixing box between exporting with reaction solution.
Preferably, described heating unit comprises the heating coil that some cylindrical shell end sockets through reactor are arranged, and is arranged on heating medium import and the thermal medium condensate outlet of reactor outside; Heating coil extends inward into the bottom in reactor, and is communicated with thermal medium condensate outlet with heating medium import respectively.
Preferably, described reactor is arranged reactor liquidometer, reactor top arranges safety valve.
Preferably, the port that described urea soln opening for feed stretches into reactor inside connects feed distributor.
Preferably, described reaction gas phase product exit is arranged on the reactor top of dividing plate downstream direction.
Compared with prior art, the present invention has following useful technique effect:
A kind of urea soln hydrolysis reactor of the present invention, by the stripper plant arranged, water vapor in stripper plant input reactor is directly contacted with urea soln, not only accelerate the hydrolysis of urea soln, and the ammonia generated in liquid phase can be accelerated constantly be diffused in gas phase, and export from reaction gas phase product exit; The setting of stripped vapor divider adds Gas-liquid interfacial area, improves hydrolysis reaction speed, can also meet the load variations needing ammonia amount on a large scale by the input and force value controlling adjustment water vapor.Can be applicable to the high efficiency extraction of existing urea solution to ammonia on the one hand, can be applicable to the extraction of urea supersaturated solution to ammonia on the other hand, ensure that hydrolysis reaction forward moves, and in the reaction liquid phase of discharging, ammonia gas dissolves is few, urea content is low.
Further, by arranging feed liquor weir plate and fluid weir plate forming reactions stripping zone, the conversion zone that stripping occurs further can be carried out retraining and limiting, and utilize the dividing plate being arranged on reaction stripping zone central authorities to extend the flow distance of reaction liquid phase, making reaction solution that sufficient Time and place can be had when reacting stripping zone flowing to be hydrolyzed reaction, while not increasing volume and energy consumption equipment, but significantly improving the efficiency of aerogenesis, urea desorption column is high, and power consumption is few.
Further, utilize the liquid mixing box arranged at urea soln opening for feed, carry out reclaiming and realizing raw material with the urea soln of urea supersaturated solution supply line supply mixing to the urea soln of the lower concentration that reaction solution outlet is discharged, make in whole reactor, under the supply of urea soln and steam, reaction gas-phase product needed for only single output, and do not react the discharge of liquid product, urea can be made to be made full use of to greatest extent, and can be random adjust according to the output of demand to ammonia of ammonia, even if ammonia output is lower also can not cause waste and meaningless consumption to urea and ammonia.Meanwhile, reduce reactor outlet water vapour content to greatest extent, and then save energy and de-mineralized water consumption.
Accompanying drawing explanation
Fig. 1 is the structural representation described in example of the present invention.
In figure: 1 is reactor, 2 is urea soln opening for feed, and 3 is heating medium import, 4 is thermal medium condensate outlet, and 5 is reaction gas phase product exit, and 6 is safety valve, 7 is stripped vapor import, and 8 is reactor liquidometer, and 9 is reaction solution outlet, 10 is heating coil, and 11 is stripped vapor divider, and 12 is dividing plate, 13 is feed liquor weir plate, 14 is fluid weir plate, and 15 is recycle pump, and 16 is liquid mixing box.
Embodiment
Below in conjunction with specific embodiment, the present invention is described in further detail, and the explanation of the invention is not limited.
As shown in Figure 1, a kind of urea soln hydrolysis reactor of the present invention, comprises the reactor 1 that bottom arranges urea soln opening for feed 2 and reaction solution outlet 9 respectively, and is arranged on the heating unit and stripper plant that set gradually along urea flow direction in reactor 1; Described reactor 1 top arranges reaction gas phase product exit 5; Described stripper plant comprises the stripped vapor import 7 being communicated with and being arranged on bottom reactor 1, and one end that reactor 1 is stretched in stripped vapor import 7 connects stripped vapor divider 11.
In use, massfraction is the urea soln of 40% ~ 60% or the supersaturated solution of urea, enters into reactor 1 by urea supply line through urea soln opening for feed 2, starts to heat up and carry out hydrolysis reaction under the heating of heating unit.The present invention is controlled the speed that ammonia produces by stripper plant, the water vapor injected through stripped vapor import 7 in stripper plant is utilized to carry out direct heating to reaction soln, and pass through to reaction stripping zone liquid phase bubbling corresponding to stripper plant in reactor 1, the ammonia being hydrolyzed generation in liquid phase is constantly diffused in gas phase go, substantially increase hydrolysis rate, can control simply and easily the output of ammonia simultaneously.
Preferably, as shown in Figure 1, in this preferred embodiment, stripper plant also comprises the dividing plate 12 be arranged on above stripped vapor divider 11, and is arranged on feed liquor weir plate 13 and the fluid weir plate 14 of divider 11 both sides; Dividing plate 12 upper end open forms gas stream and opens one's mouth, and lower ending opening forms liquid stream and opens one's mouth; Feed liquor weir plate 13 is arranged on the updrift side of dividing plate 12, and upper end open forms liquid inflow port; Fluid weir plate 14 is arranged on the downstream direction of dividing plate 12, and upper end open forms overflow mouth; Forming reactions stripping zone between feed liquor weir plate 13 and fluid weir plate 14.Further, urea soln opening for feed 2 is communicated with urea soln supply line by a feed end of liquid mixing box 16; Another feed end and the reaction solution of liquid mixing box 16 export 9 and are communicated with.Further, liquid mixing box 16 and reaction solution export between 9 and are also provided with for reaction solution being added the recycle pump 15 of pressing and being injected in liquid mixing box 16.Thus hydrolysis reactor inside forms circulation, externally can not produce the discharge of waste, utilising efficiency is high, and aerogenesis is effective.
Preferably, as shown in Figure 1, heating unit comprises the heating coil 10 that some cylindrical shell end sockets through reactor 1 are arranged, and is arranged on heating medium import 3 and the thermal medium condensate outlet 4 of reactor 1 outside; Heating coil 10 extends inward into the bottom in reactor 1, and is communicated with thermal medium condensate outlet 4 with heating medium import 3 respectively; This preferred embodiment is described for U-shaped heating coil; Reactor 1 is arranged reactor liquidometer 8, liquid level in reactor 1 can be shown and reach quantitative value, thus control the input of urea soln; Reactor 1 top arranges safety valve 6, ensures the use safety of pressure-vessel reactor 1; The port that urea soln opening for feed 2 stretches into reactor 1 inside connects feed distributor; Urea soln can be made through feed distributor, uniform and heating coil 10 heat exchange of the urea soln that enters to be heated up; Reaction gas phase product exit 5 is arranged on reactor 1 top of dividing plate 12 downstream direction, better can ensure the smooth discharge of ammonia.
Reaction stripping zone is set in urea soln hydrolysis reactor of the present invention, accelerate hydrolysate by steam to be separated from liquid phase, urea concentration after reaction stripping zone reduces, the urea soln of low concentration is transported to liquid mixing box by recycle pump, after the supersaturation urea soln come with urea soln preparation system mixes, return hydrolysis reactor.Can not only realize fast to the urea soln of existing concentration efficiently, controlled hydrolysis reaction, well can also be applicable to the hydrolysis reaction of the urea soln of high density, efficient and controlled object can be reached equally, and can be further, make inside reactor do not remove required gas-phase product discharge outside other waste products, by the hydrolysis to high concentration urea solution, also reduce the content of water vapor in gas-phase product, save the energy greatly, reasonable in design, structure is ingenious, safe and reliable, high-efficiency environment friendly, react controlled, reduce energy consumption, urea and energy utilization rate high.
Claims (7)
1. a urea soln hydrolysis reactor, it is characterized in that, comprise the reactor (1) that bottom arranges urea soln opening for feed (2) and reaction solution outlet (9) respectively, and be arranged on the interior heating unit that sets gradually along urea flow direction of reactor (1) and stripper plant; Described reactor (1) top arranges reaction gas phase product exit (5); Described stripper plant comprises the stripped vapor import (7) that connection is arranged on reactor (1) bottom, one end that reactor (1) is stretched in stripped vapor import (7) connects stripped vapor divider (11), and described urea soln opening for feed (2) is communicated with urea soln supply line by a feed end of liquid mixing box (16); Another feed end of liquid mixing box (16) exports (9) and is communicated with reaction solution.
2. a kind of urea soln hydrolysis reactor according to claim 1, it is characterized in that, described stripper plant also comprises the dividing plate (12) being arranged on stripped vapor divider (11) top, and is arranged on feed liquor weir plate (13) and the fluid weir plate (14) of divider (11) both sides; Dividing plate (12) upper end open forms gas stream and opens one's mouth, and lower ending opening forms liquid stream and opens one's mouth; Feed liquor weir plate (13) is arranged on the updrift side of dividing plate (12), and upper end open forms liquid inflow port; Fluid weir plate (14) is arranged on the downstream direction of dividing plate (12), and upper end open forms overflow mouth; Forming reactions stripping zone between feed liquor weir plate (13) and fluid weir plate (14).
3. a kind of urea soln hydrolysis reactor according to claim 1, it is characterized in that, described liquid mixing box (16) exports with reaction solution to be also provided with between (9) and is injected into recycle pump (15) in liquid mixing box (16) for reaction solution being added pressure.
4. a kind of urea soln hydrolysis reactor according to claim 1, it is characterized in that, described heating unit comprises the heating coil (10) that some cylindrical shell end sockets through reactor (1) are arranged, and is arranged on the outside heating medium import (3) of reactor (1) and thermal medium condensate outlet (4); Heating coil (10) extends inward into the bottom in reactor (1), and is communicated with thermal medium condensate outlet (4) with heating medium import (3) respectively.
5. a kind of urea soln hydrolysis reactor according to claim 1, is characterized in that, described reactor (1) arranges reactor liquidometer (8), and reactor (1) top arranges safety valve (6).
6. a kind of urea soln hydrolysis reactor according to claim 1, is characterized in that, described urea soln opening for feed (2) stretches into the inner port of reactor (1) and connects feed distributor.
7. a kind of urea soln hydrolysis reactor according to claim 1, is characterized in that, described reaction gas phase product exit (5) is arranged on reactor (1) top of dividing plate (12) downstream direction.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310400325.4A CN103482649B (en) | 2013-09-05 | 2013-09-05 | Urea solution hydrolysis reactor |
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|---|---|---|---|
| CN201310400325.4A CN103482649B (en) | 2013-09-05 | 2013-09-05 | Urea solution hydrolysis reactor |
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| CN103482649A CN103482649A (en) | 2014-01-01 |
| CN103482649B true CN103482649B (en) | 2015-06-17 |
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| CN201310400325.4A Expired - Fee Related CN103482649B (en) | 2013-09-05 | 2013-09-05 | Urea solution hydrolysis reactor |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103950954B (en) * | 2014-05-13 | 2016-06-22 | 西安丹辉环保科技有限公司 | A kind of enclosed heats the method for small-sized hydrolysis of urea reaction unit and hydrolysis |
| CN107188198A (en) * | 2017-06-28 | 2017-09-22 | 西安热工研究院有限公司 | A kind of thermal power plant's denitration is pyrolyzed with hydrolysis of urea and is combined ammonia system processed |
| CN114405450A (en) * | 2022-02-23 | 2022-04-29 | 西安热工研究院有限公司 | Filling type urea catalytic hydrolysis device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030118494A1 (en) * | 2001-12-21 | 2003-06-26 | Environmental Elements Corporation | Process and apparatus for conditioning of combustion flue gases with ammonia from hydrolyzed urea |
| CN101182063A (en) * | 2007-10-29 | 2008-05-21 | 太原海力丰科技发展有限公司 | Method for purifying carbamide polluted water |
| CN102167412A (en) * | 2011-04-08 | 2011-08-31 | 吉林化工学院化工分离技术开发中心 | High-efficiency composite urea waste liquid deep hydrolysis desorption tower |
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2013
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030118494A1 (en) * | 2001-12-21 | 2003-06-26 | Environmental Elements Corporation | Process and apparatus for conditioning of combustion flue gases with ammonia from hydrolyzed urea |
| CN101182063A (en) * | 2007-10-29 | 2008-05-21 | 太原海力丰科技发展有限公司 | Method for purifying carbamide polluted water |
| CN102167412A (en) * | 2011-04-08 | 2011-08-31 | 吉林化工学院化工分离技术开发中心 | High-efficiency composite urea waste liquid deep hydrolysis desorption tower |
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