CN103482649A - Urea solution hydrolysis reactor - Google Patents
Urea solution hydrolysis reactor Download PDFInfo
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- CN103482649A CN103482649A CN201310400325.4A CN201310400325A CN103482649A CN 103482649 A CN103482649 A CN 103482649A CN 201310400325 A CN201310400325 A CN 201310400325A CN 103482649 A CN103482649 A CN 103482649A
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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 processed 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 accompanied by a large amount of oxynitride (NO
x) discharge, atmosphere is polluted.Usually take to add equipment for denitrifying flue gas at boiler tail, utilize selective catalytic reduction (SCR) to remove the NO in flue gas
x, be translated into nontoxic nitrogen (N
2) and water (H
2o), thus reach emission request.Required denitrification reducing agent ammonia (NH in selective catalytic reduction
3) three kinds of supply forms are arranged usually: liquefied ammonia, ammoniacal liquor and urea.Wherein, liquefied ammonia and ammoniacal liquor belong to hazardous chemical.There are strict legal provisions in country in the storage that relates to liquefied ammonia and ammoniacal liquor, use and transportation.And industrial urea is white crystals body particle, do not belong to the hazardous chemical category, be convenient to store and transportation, can not cause potential safety hazard because of leakage, therefore from the safety and economy angle, consider, urea ammonia processed is subject to people's favor gradually, realizes the supply of ammonia by the urea soln hydrolysis method that adopts one of urea ammonia method processed.
In existing urea soln hydrolysis reactor, when urea soln injects, consider the solubleness of urea under normal temperature and the security of course of conveying, what all adopt is the urea soln that massfraction is 40%-60%; Chemical equation according to hydrolysis of urea
suppose urea soln mass concentration 50%, calculate according to the stoichiometric ratio of hydrolysis of urea reaction to only have the water of solution weight 15% to participate in chemical reaction, all the other water that account for urea soln weight 35% do not participate in hydrolysis reaction.This excessive water of 35%, after the heat absorption vaporization, leaves reactor with reaction product, causes the waste of energy and the desalination water yield.Suppose urea soln mass concentration 60%, calculate according to the stoichiometric ratio of hydrolysis of urea reaction to only have the water of solution weight 18% to participate in chemical reaction, all the other water that account for urea soln weight 22% do not participate in hydrolysis reaction.
If urea and water are configured to urea soln according to hydrolysis reaction metering ratio, the mass concentration of urea soln need to reach 77%, the urea soln of this concentration must be the supersaturated solution of urea, therefore carry out liquid using the supersaturated solution of urea as hydrolysis reactor, will greatly reduce the content of reactor outlet water vapor, but existing reactor all can't meet the processing requirement of accepting the urea supersaturated solution, and 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 the urea supersaturated solution as carrying out liquid, reduces the reactor outlet vapour content, thereby saves energy and desalination water consumption.
The present invention is achieved through the following technical solutions:
A kind of urea soln hydrolysis reactor, comprise that bottom arranges respectively the reactor of urea soln opening for feed and reaction solution outlet, and be arranged on heating unit and the stripper plant set gradually along the urea flow direction in reactor; Described reactor top arranges the outlet of reaction gas-phase product; Described stripper plant comprises that connection is arranged on the stripped vapor import of reactor bottom, and the end that reactor is stretched in the stripped vapor import connects the stripped vapor divider.
Preferably, described stripper plant also comprises the dividing plate that is arranged on stripped vapor divider top, and the feed liquor weir plate and the fluid weir plate that are arranged on the divider both sides; The dividing plate upper end open forms gas stream and opens one's mouth, and lower ending opening forms the liquid-flow mouth; The feed liquor weir plate is arranged on the updrift side of dividing plate, and upper end open forms the liquid influx; The fluid weir plate is arranged on the downstream direction of dividing plate, and upper end open forms the overflow mouth; Form the reaction stripping zone between feed liquor weir plate and fluid weir plate.
Preferably, described urea soln opening for feed is communicated with the urea soln supply line by a feed end of liquid mixing box; Another feed end of liquid mixing box is communicated with the reaction solution outlet.
Further, between described liquid mixing box and reaction solution outlet, also be provided with for the reaction solution addition being pressed to the recycle pump that is injected into liquid mixing box.
Preferably, described heating unit comprises the heating coil that some cylindrical shell end sockets through reactor arrange, and the heating medium import and the thermal medium condensate outlet that are arranged on the reactor outside; Heating coil extends inward into the bottom in reactor, and with heating medium import and thermal medium condensate outlet, is communicated with respectively.
Preferably, the reactor liquidometer is set on described reactor, the reactor top arranges safety valve.
Preferably, described urea soln opening for feed stretches into the port connection feed distributor of reactor inside.
Preferably, described reaction gas-phase product outlet 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 accelerated the hydrolysis of urea soln, and the ammonia that can accelerate to generate in the liquid phase constantly is diffused in gas phase, and output from the outlet of reaction gas-phase product; Arranging of stripped vapor divider increased Gas-liquid interfacial area, improves hydrolysis reaction speed, and input and the force value that can also adjust water vapor by control meet the load variations that needs on a large scale the ammonia amount.Can be applicable to the high efficiency extraction of existing urea solution to ammonia on the one hand, can be applicable on the other hand the extraction of urea supersaturated solution to ammonia, guarantee that the hydrolysis reaction forward moves, and in the reaction liquid phase of discharging, ammonia dissolves less, urea content is low.
Further, by being set, feed liquor weir plate and fluid weir plate form the reaction stripping zone, the conversion zone that stripping can be occurred is further retrained and is limited, and utilize the dividing plate that is arranged on reaction stripping zone central authorities to extend the mobile distance of reaction liquid phase, make reaction solution that the reaction that is hydrolyzed of sufficient time and space can be arranged when the reaction stripping zone flows, when not increasing volume and energy consumption equipment, but significantly promoted the efficiency of aerogenesis, the urea utilization ratio is high, and power consumption is few.
Further, the liquid mixing box that utilization arranges at the urea soln opening for feed, the urea soln of the lower concentration that outlet is discharged to reaction solution is reclaimed and is realized that with the urea soln of urea supersaturated solution supply line supply raw material mixes, make in whole reactor, under the supply of urea soln and steam, the required reaction gas-phase product of single output only, and do not react the discharge of liquid product, can make urea be taken full advantage of to greatest extent, and the demand according to ammonia that can be random is adjusted the output of ammonia, can not cause waste and meaningless consumption to urea and ammonia even the ammonia output is low yet.Simultaneously, reduce to greatest extent the reactor outlet water vapour content, and then save energy and de-mineralized water consumption.
The accompanying drawing explanation
Fig. 1 is the structural representation described in example of the present invention.
In figure: 1 is reactor, and 2 is the urea soln opening for feed, and 3 is the heating medium import, 4 is the thermal medium condensate outlet, and 5 is the outlet of reaction gas-phase product, and 6 is safety valve, 7 is the stripped vapor import, and 8 is the reactor liquidometer, and 9 is the reaction solution outlet, 10 is heating coil, and 11 is the stripped vapor divider, and 12 is dividing plate, 13 is the feed liquor weir plate, 14 is the 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, comprise that bottom arranges respectively the reactor 1 of urea soln opening for feed 2 and reaction solution outlet 9, and be arranged on the interior heating unit set gradually along the urea flow direction of reactor 1 and stripper plant; Described reactor 1 top arranges reaction gas-phase product outlet 5; Described stripper plant comprises that connection is arranged on the stripped vapor import 7 of reactor 1 bottom, and the end that reactor 1 is stretched in stripped vapor import 7 connects stripped vapor divider 11.
In use, the urea soln that massfraction is 40%～60% or the supersaturated solution of urea, enter into reactor 1 by the urea supply line through urea soln opening for feed 2, starts to heat up under the heating of heating unit and carry out hydrolysis reaction.The speed that the present invention produces ammonia by stripper plant is controlled, utilize the water vapor injected through stripped vapor import 7 in stripper plant to carry out direct heating to reaction soln, and by the reaction stripping zone liquid phase bubbling corresponding to the interior stripper plant of reactor 1, make the ammonia that in liquid phase, hydrolysis produces constantly be diffused in gas phase and go, greatly improved 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 that is arranged on stripped vapor divider 11 tops, and the feed liquor weir plate 13 and the fluid weir plate 14 that are arranged on divider 11 both sides; Dividing plate 12 upper end open form gas stream and open one's mouth, and lower ending opening forms the liquid-flow mouth; Feed liquor weir plate 13 is arranged on the updrift side of dividing plate 12, and upper end open forms the liquid influx; Fluid weir plate 14 is arranged on the downstream direction of dividing plate 12, and upper end open forms the overflow mouth; Form the reaction stripping zone between feed liquor weir plate 13 and fluid weir plate 14.Further, urea soln opening for feed 2 is communicated with the urea soln supply line by a feed end of liquid mixing box 16; Another feed end of liquid mixing box 16 is communicated with reaction solution outlet 9.Further, between liquid mixing box 16 and reaction solution outlet 9, also be provided with for the reaction solution addition being pressed to the recycle pump 15 that is injected into liquid mixing box 16.Thereby inner formation of hydrolysis reactor circulated, and externally can not produce the discharge of waste, and 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 arrange, and the heating medium import 3 and the thermal medium condensate outlet 4 that are arranged on reactor 1 outside; Heating coil 10 extends inward into the bottom in reactor 1, and with heating medium import 3 and thermal medium condensate outlet 4, is communicated with respectively; This preferred embodiment be take U-shaped heating coil and is described as example; Reactor liquidometer 8 is set on reactor 1, can shows that the interior liquid level of reactor 1 reaches quantitative value, thereby control the input of urea soln; Reactor 1 top arranges safety valve 6, guarantees 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; Can make urea soln through feed distributor make the urea soln that enters uniformly with heating coil 10 heat exchange intensifications; Reaction gas-phase product outlet 5 is arranged on reactor 1 top of dividing plate 12 downstream directions, can better guarantee the smooth discharge of ammonia.
In urea soln hydrolysis reactor of the present invention, the reaction stripping zone is set, accelerate hydrolysate by steam separates from liquid phase, urea concentration after the 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 the urea soln preparation system mixes, return to hydrolysis reactor.Not only can to the urea soln of existing concentration, realize fast efficiently, controlled hydrolysis reaction, can also well be applicable to the hydrolysis reaction of the urea soln of high density, can reach efficient and controlled purpose equally, and can be further, make inside reactor not remove required gas-phase product and discharge other outer waste products, by the hydrolysis to high concentration urea solution, also reduced the content of water vapor in the gas-phase product, saved greatly the energy, reasonable in design, structure is ingenious, safe and reliable, high-efficiency environment friendly, react controlled, reduce energy consumption, urea and energy utilization rate are high.
Claims (8)
1. a urea soln hydrolysis reactor, it is characterized in that, comprise that bottom arranges respectively the reactor (1) of urea soln opening for feed (2) and reaction solution outlet (9), and be arranged on heating unit and the stripper plant set gradually along the urea flow direction in reactor (1); Described reactor (1) top arranges reaction gas-phase product outlet (5); Described stripper plant comprises that connection is arranged on the stripped vapor import (7) of reactor (1) bottom, and the end that reactor (1) is stretched in stripped vapor import (7) connects stripped vapor divider (11).
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) that is arranged on stripped vapor divider (11) top, and the feed liquor weir plate (13) and the fluid weir plate (14) that are arranged on divider (11) both sides; Dividing plate (12) upper end open forms gas stream and opens one's mouth, and lower ending opening forms the liquid-flow mouth; Feed liquor weir plate (13) is arranged on the updrift side of dividing plate (12), and upper end open forms the liquid influx; Fluid weir plate (14) is arranged on the downstream direction of dividing plate (12), and upper end open forms the overflow mouth; Form the reaction 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 and 2, is characterized in that, described urea soln opening for feed (2) is communicated with the urea soln supply line by a feed end of liquid mixing box (16); Another feed end of liquid mixing box (16) is communicated with reaction solution outlet (9).
4. a kind of urea soln hydrolysis reactor according to claim 3, is characterized in that, between described liquid mixing box (16) and reaction solution outlet (9), also is provided with for the reaction solution addition being pressed to the recycle pump (15) that is injected into liquid mixing box (16).
5. 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) arrange, and is arranged on reactor (1) outside heating medium import (3) and thermal medium condensate outlet (4); Heating coil (10) extends inward into the bottom in reactor (1), and with heating medium import (3) and thermal medium condensate outlet (4), is communicated with respectively.
6. a kind of urea soln hydrolysis reactor according to claim 1, is characterized in that, reactor liquidometer (8) is set on described reactor (1), and reactor (1) top arranges safety valve (6).
7. 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.
8. a kind of urea soln hydrolysis reactor according to claim 1, is characterized in that, described reaction gas-phase product outlet (5) is arranged on reactor (1) top of dividing plate (12) downstream direction.
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| 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 true CN103482649A (en) | 2014-01-01 |
| CN103482649B CN103482649B (en) | 2015-06-17 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103950954A (en) * | 2014-05-13 | 2014-07-30 | 西安丹辉环保科技有限公司 | Embraced-type heating small urea hydrolysis reaction device and hydrolysis method thereof |
| 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 |
| CN113426153A (en) * | 2021-06-25 | 2021-09-24 | 中国成达工程有限公司 | Production device and method for producing urea for liquid vehicle and urea solution for denitration |
| 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 |
-
2013
- 2013-09-05 CN CN201310400325.4A patent/CN103482649B/en not_active Expired - Fee Related
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 |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103950954A (en) * | 2014-05-13 | 2014-07-30 | 西安丹辉环保科技有限公司 | Embraced-type heating small urea hydrolysis reaction device and hydrolysis method thereof |
| 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 |
| CN113426153A (en) * | 2021-06-25 | 2021-09-24 | 中国成达工程有限公司 | Production device and method for producing urea for liquid vehicle and urea solution for denitration |
| 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 |
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| CN103482649B (en) | 2015-06-17 |
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