CN105129818A - Double air chamber heated urea catalytic hydrolysis reactor and method - Google Patents
Double air chamber heated urea catalytic hydrolysis reactor and method Download PDFInfo
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- CN105129818A CN105129818A CN201510487560.9A CN201510487560A CN105129818A CN 105129818 A CN105129818 A CN 105129818A CN 201510487560 A CN201510487560 A CN 201510487560A CN 105129818 A CN105129818 A CN 105129818A
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Abstract
The invention discloses a double air chamber heated urea catalytic hydrolysis reactor and a method. The urea catalytic hydrolysis reactor comprises a reaction chamber and a sewage discharge chamber. The liquid level of the reaction chamber is raised regularly to discharge the upper layer sewage containing liquid into the sewage discharge chamber, the blowdown liquid is subjected to secondary decomposition in the sewage discharge chamber and then discharged, and the two chambers are both equipped with a heating coil, thus achieving sewage discharge and efficient use of energy.
Description
Technical field
The invention belongs to technical field of air pollution control, relate to the hydrolysis reactor that a kind of ammonia utilizing urea seeding to be hydrolyzed generation makes coal-fired power plant denitrating flue gas, be specifically related to urea seeding hydrolysis reactor and the method for a kind of pair of air chamber heating.
Technical background
Denitrating flue gas, refer to the technology removed by objectionable impurities-NOX contained in the flue gas that (comprises coal firing boiler, oil-burning gas-fired boiler and some industrial furnaces) after high-temp combustion, comprise SCR and SNCR two kinds of major technique schools, wherein SCR is the mainstream technology of denitrating flue gas.So-called SCR technology, refer to and SCR reactor is set between the economizer and air preheater of boiler, in reactor, install catalyzer, spray into reductive agent (ammonia-containing gas) in the flue cross section before reactor, reductive agent and NOX react and remove NOX on catalyst surface.
The reductive agent that SCR denitrating flue gas uses is ammonia essentially, need to arrange at the scene a set of can the device of continuous production ammonia.From raw material, ammonia preparation system can be divided into anhydrous liquid ammonia system, ammoniacal liquor system and urea system.Wherein use the system of liquefied ammonia Evaporation preparation ammonia the most conventional, reason is that its investment is the most cheap, and transport, use cost are also minimum, but there is great potential safety hazard in liquefied ammonia system, particularly its transport and storage process, the harm that A leak of liquefied ammonia brings is very large, and security incident is of common occurrence; The investment of ammoniacal liquor system, operation and transportation cost are all very high, more safe than liquefied ammonia, but still have certain potential safety hazard; The investment of urea system and running cost height compared with liquefied ammonia system, but transportation cost is suitable, and urea system there is no potential safety hazard, is safest ammonia technology of preparing.
The process for producing ammonia from urea technology of current commercial applications mainly contains hydrolysis of urea and urea pyrolysis, wherein hydrolysis of urea includes again the catalytic hydrolysis (SafeDeNOx) of common hydrolysis (AOD, U2A, domestic chemical industry hydrolysis) and U.S. Chemithon, the urea pyrolysis then mainly NOxOUTULTRA technology that provides of American Fuel company (Fueltech).
The soonest and the safest, the on-the-spot container almost not storing up ammonia, its energy consumption and working cost are very high, so comparatively early enter Chinese market, achievement is more, but in today of oil price height enterprise, though there is application, the running cost pressure of single user is very large for the speed of response of pyrolysis.Compare with pyrolysis, be hydrolyzed owing to adopting power plant compared with the steam of horn of plenty as thermal source, energy consumption is lower.But the external technology for hydrolyzing such as AOD, U2A, reaction is comparatively slow needs huge reactor and snubber assembly, its investment and energy consumption higher.The speed of response of catalytic hydrolysis is also very fast, and start-stop is rapid, and energy consumption is lower, but this technology is not also very ripe comparatively speaking, there is no application at home.But if develop ripe urea seeding technology for hydrolyzing, the safety and stability ammonia sources required for SCR denitration device of domestic extensive installation can not only be met, a large amount of energy can also be saved, realize harmony that is energy-conservation and environmental protection.
But under the effect not having catalyzer, this speed of response is comparatively slow, is difficult to meet the corresponding requirement of load.If can by adding effective catalyzer, significantly improving hydrolysis reaction speed, then not only can meet load corresponding requirements, and due to the raising of speed, reduce the requirement to hydrolysis device capacity surge capability, significantly can reduce facility investment.But existing urea seeding hydrolysis device does not consider the process of impurity, cleaning difficulty, high to urea purity requirement, this adds increased operation cost.
Summary of the invention
For shortcomings and deficiencies of the prior art, the object of this invention is to provide urea seeding hydrolysis reactor and the method for a kind of pair of air chamber heating, comprise the two air chamber of reaction chamber and blowdown room, and these two air chambers are all provided with heating coil, realize effective utilization of blowdown and the energy.
Technical scheme of the present invention is as follows:
A urea seeding hydrolysis reactor for pair air chamber heating, comprises the reaction chamber and these two air chambers of blowdown room that are separated by baffle plate, and the height of described plate washer is higher than the half of height for reactor, and the bottom of these two air chambers is all provided with heating coil.
Preferably, the height of described plate washer is the 60%-80% of urea seeding hydrolysis reactor height.
Further, described reaction chamber comprises at least two temperature sensors, thermometer, tensimeter, pressure transmitter, two radar level gauges, a liquidometer on the spot on the spot on the spot; Described blowdown room comprises at least one temperature sensor, radar level gauge, a liquidometer on the spot.
Further, described blowdown room is provided with blowdown room sewage draining exit, and the installation site of liquidometer on the spot of described blowdown room is as far as possible close to described blowdown room sewage draining exit.
Further, the liquidometer on the spot of described reaction chamber and blowdown room adopts steam jacket companion heat, and useful range should be able to meet that urea seeding hydrolysis reactor is the highest, minimum liquid level requirement, and bore must not lower than 100mm.
Further, described reaction chamber is provided with urea soln import and reaction chamber sewage draining exit, described urea soln import and reaction chamber sewage draining exit lay respectively at reaction chamber both sides, described reaction chamber sewage outfalls setting is in reaction chamber lower-most point, described urea soln import is arranged on above described heating coil, runs below liquid level.
Further, be provided with catalyst inlet above described reaction chamber, described catalyst inlet be connected with catalyst inlet pipe, described catalyst inlet pipe is embedded to and runs in liquid level.
Further, described urea seeding hydrolysis reactor is provided with product gas outlet, described product gas outlet place is configured with steam separator, steam separator mainly utilizes gas different with the density of liquid, and by expanding pipeline latus rectum, reduction speed also changes the direction of speed, make the drop separation of gas product and entrained with, reduce liquid to the corrosion of subsequent pipeline, equipment, improve the quality of gas product, steam separator is processing and fabricating together with reactor.
Further, described reaction chamber is also provided with thief hole, for carrying out sampling and testing to the sample in reaction chamber.
Adopt a urea seeding method for hydrolysis for above-mentioned reactor, comprise the following steps:
1) in reaction chamber, de-mineralized water is added, to 25% of chamber volume;
2) catalyzer being dissolved in urea soln is added reaction chamber;
3) urea soln is added reaction chamber, make liquid level reach 50% of chamber volume, heating is reacted;
4) regularly improving reaction chamber liquid level to exceeding plate washer height, making the floating matter above liquid level be drained into blowdown room through plate washer, after continuing reaction for some time, the impurity bottom reaction chamber and blowdown room being discharged;
5) gas product that reaction generates carries out, after gas-liquid separation, being discharged by product gas outlet through steam separator.
Further, step 3) in add reaction chamber urea concentration be no more than 28%.
Beneficial effect of the present invention is as follows:
Because urea and catalyzer contain the pollutent produced in impurity, reaction process, so need solid, settling and other pollutents in timing cleaning reactor, it is made to be retained to minimum value, namely reactor needs regularly to carry out bottom blow-down and surface blow-off, in order to realize good surface blow-off and the twice decomposition of blowdown, the application devises two air chamber: reaction chamber and blowdown room.The liquid level of regular rising reaction chamber, enters blowdown room by upper strata containing soiling solution body, carries out twice decomposition, then discharge reactor containing soiling solution body in blowdown room.Which increase urea desorption column, through the test of third party northeast DianKeYuan, based on the engineering mimoir of achievement in research 200MW thermoelectricity unit denitrating system 150KG/h ammonia amount, ammonia system percent hydrolysis 99.53% processed, considerably reduces blowdown loss.
Accompanying drawing explanation
Fig. 1 is the structural representation of the urea seeding hydrolysis reactor embodiment of a kind of pair of air chamber heating provided by the invention.
In figure: 1-blowdown room; 2-plate washer; 3-reaction chamber; 4-blowdown room heating coil; 5-reaction chamber heating coil; 6-steam separator; The import of N1-urea soln; N2-catalyst inlet; N3-product gas outlet; N4-reaction chamber sewage draining exit; N5-relief valve port; N6-reserved opening (reaction chamber thief hole); N11-blowdown room sewage draining exit; T1, T2, T4-teletransmission Temperature displaying; T3-is Temperature displaying on the spot; L1, L2, L6, L7-liquid level display on the spot; L3, L4, L5-remote liquid level shows; P1, P2-differential manometer mouth; P3-teletransmission pressure shows; P4-shows with regard to ground pressure; M-manhole.
Embodiment
Below in conjunction with accompanying drawing, structure of the present invention, principle and working process are further described.
Embodiment 1
As shown in Figure 1, the urea seeding hydrolysis reactor of provided by the invention pair of air chamber heating contains blowdown room 1; Plate washer 2; Reaction chamber 3.In this embodiment, the volume of urea seeding hydrolysis reactor is 5.9 cubic metres, high 1400mm, and the height of plate washer is 980mm, because the liquid level inside reactor will be the half of height for reactor, the height of plate washer should higher than the half of height for reactor.The bottom of blowdown room 1 and reaction chamber 3 is all provided with U-shaped heating coil, and the liquid level now inside reactor should higher than U-shaped heating coil.
The first step: the de-mineralized water being added 25% (by volume calculating) by urea soln import N1 in Empty reactor enters reaction chamber 3, makes liquid level reach 350mm.
Second step: a certain amount of catalyzer (such as, ratio is reactor volume 7% phosphoric acid salt catalyzer) being dissolved in urea soln is entered reaction chamber 3 by catalyst inlet N2.
3rd step: the urea soln of mass percentage 50% is entered reaction chamber 3 by urea soln import N1, make liquid level reach 700mm (to 50% of reactor 3 volume), now in reactor 3, the starting point concentration of urea is approximately 25%.Because water first dilutes out during heating, solution can be more and more denseer, and the urea concentration that in reactor 3, Initial dilution starts must not more than 28%.
Liquid level is improved (more than 980mm) by reaction for some time (such as a week), the floating matter above liquid level is made to be drained into blowdown room 1 through plate washer 2, in experience for some time, the impurity bottom reaction chamber 3 and blowdown room 1 is discharged by reaction chamber sewage draining exit N4 and blowdown room sewage draining exit N11, wherein blowdown liquid is discharged by blowdown room sewage draining exit N11, and the liquid bottom reaction chamber 3 is discharged by reaction chamber sewage draining exit N4.
Blowdown room heating coil 4 and reaction chamber heating coil 5 heat the solution of blowdown room 1 and reaction chamber 3 respectively.Teletransmission Temperature displaying T1, T2, T4 and on the spot Temperature displaying T3; Liquid level display L1, L2, L6, L7 on the spot; Remote liquid level display L3, L4, L5; Differential manometer mouth P1, P2, teletransmission pressure shows P3 and characterizes temperature, liquid level and the pressure of reaction chamber and blowdown room with regard to ground pressure display P4 respectively.
Gas product (ammonia, carbonic acid gas, water vapour) is after steam separator 6 carries out gas-liquid separation, and gas is discharged by product gas outlet N3.Reserved opening N6 also can be used as thief hole simultaneously, carries out sampling and testing as required, in addition, steam separator 6 is also provided with relief valve port N5 to the sample in reaction chamber 3.
Manhole M is also provided with above reaction chamber 3.
Claims (10)
1. a urea seeding hydrolysis reactor for two air chamber heating, comprises the reaction chamber and these two air chambers of blowdown room that are separated by baffle plate, and the height of described plate washer is higher than the half of height for reactor, and the bottom of these two air chambers is all provided with heating coil.
2. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, it is characterized in that, the height of described plate washer is the 60%-80% of urea seeding hydrolysis reactor height.
3. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, it is characterized in that, the reaction chamber of described urea seeding hydrolysis reactor comprises at least two temperature sensors, thermometer, tensimeter, pressure transmitter, two radar level gauges, a liquidometer on the spot on the spot on the spot; Described blowdown room comprises at least one temperature sensor, radar level gauge, a liquidometer on the spot.
4. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 3, it is characterized in that, described blowdown room is provided with blowdown room sewage draining exit, and the installation site of liquidometer on the spot of described blowdown room is close to described blowdown room sewage draining exit; The liquidometer on the spot of described reaction chamber and blowdown room adopts steam jacket companion heat, and useful range meets that urea seeding hydrolysis reactor is the highest, minimum liquid level requirement, and bore is not less than 100mm.
5. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, it is characterized in that, described reaction chamber is provided with urea soln import and reaction chamber sewage draining exit, described urea soln import and reaction chamber sewage draining exit lay respectively at reaction chamber both sides, described reaction chamber sewage outfalls setting is in reaction chamber lower-most point, described urea soln import is arranged on above described heating coil, runs below liquid level.
6. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, it is characterized in that, be provided with catalyst inlet above described reaction chamber, described catalyst inlet be connected with catalyst inlet pipe, the inlet pipe of described catalyzer is embedded to and runs in liquid level.
7. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, it is characterized in that, described urea seeding hydrolysis reactor is provided with product gas outlet, and described product gas outlet place is configured with the steam separator of the drop separation for making gas product and entrained with.
8. the urea seeding hydrolysis reactor of two air chamber heating as claimed in claim 1, is characterized in that, described reaction chamber is also provided with thief hole, for carrying out sampling and testing to the sample in reaction chamber.
9. adopt the urea seeding method for hydrolysis of the urea seeding hydrolysis reactor of the arbitrary described two air chamber heating of claim 1-8, comprise the following steps:
1) in reaction chamber, de-mineralized water is added, to 25% of chamber volume;
2) catalyzer being dissolved in urea soln is added reaction chamber;
3) urea soln is added reaction chamber, make liquid level reach 50% of chamber volume, heating is reacted;
4) regularly improving reaction chamber liquid level to exceeding plate washer height, making the floating matter above liquid level be drained into blowdown room through plate washer, after continuing reaction for some time, the impurity bottom reaction chamber and blowdown room being discharged;
5) gas product that reaction generates carries out, after gas-liquid separation, being discharged by product gas outlet through steam separator.
10. urea seeding method for hydrolysis as claimed in claim 9, is characterized in that, step 3) in add reaction chamber urea concentration be no more than 28%.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103395801A (en) * | 2013-08-08 | 2013-11-20 | 中国大唐集团环境技术有限公司 | Method and device for catalytic hydrolysis of urea |
| CN104560072A (en) * | 2014-12-26 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis system and pyrolysis method for organic wastes |
| CN204529332U (en) * | 2015-04-10 | 2015-08-05 | 重庆远达烟气治理特许经营有限公司 | Stir adjustable hydrolysis of urea reactor |
| CN205061580U (en) * | 2015-08-10 | 2016-03-02 | 大唐环境产业集团股份有限公司 | Urea seeding hydrolysis reactor of two air chambers heating |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103395801A (en) * | 2013-08-08 | 2013-11-20 | 中国大唐集团环境技术有限公司 | Method and device for catalytic hydrolysis of urea |
| CN104560072A (en) * | 2014-12-26 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis system and pyrolysis method for organic wastes |
| CN204529332U (en) * | 2015-04-10 | 2015-08-05 | 重庆远达烟气治理特许经营有限公司 | Stir adjustable hydrolysis of urea reactor |
| CN205061580U (en) * | 2015-08-10 | 2016-03-02 | 大唐环境产业集团股份有限公司 | Urea seeding hydrolysis reactor of two air chambers heating |
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