CN103387292A - Boiler supply water oxygenation process - Google Patents
Boiler supply water oxygenation process Download PDFInfo
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Abstract
The invention discloses a boiler supply water oxygenation process. The phases of supply water oxygenation comprise a preliminary oxygenation phase and a later oxygenation phase; a transition point of the two phases is 12 months after beginning of supply water oxygenation; in the first month of the preliminary oxygenation phase, oxygen supply amounts at the outlet of a condensate polishing system and at the outlet of a deoxygenator are controlled in a range of 35 to 40 mu g/L and are then gradually reduced at an amplitude of 0.01 to 0.03%/month; in the later oxygenation phase, oxygen supply amounts at the outlet of the condensate polishing system and at the outlet of the deoxygenator are both controlled to be less than 30 mu g/L, a hydrogen amount at the inlet of the deoxygenator is stably controlled in a range of 0.2 to 0.4 mu g/L, and a hydrogen amount in main steam is stably controlled in a range of 0.4 to 0.8 mu g/L. The process provided by the invention can utmostly inhibit disadvantages of oxygenation on the basis of full usage of the advantages of oxygenation, effectively prevents tube explosion caused by falling of oxide skin and guarantees security, reliability and economical efficiency of boiler operation.
Description
Technical field
The present invention relates to the oiler feed processing technology field, especially relate to a kind of oiler feed oxygenation treatment process.
Background technology
Under boiler volatilized the anaerobic of processing, high pH value operating mode entirely, mobile accelerated corrosion (FAC) easily occurred in feedwater, draining system, and economizer, water wall sedimentation rate are high.And produce thus a series of problem, cause unit boiler pressure reduction to rise as fouling fast; The service pump power consumption is high; Desuperheating water regulating valve, drain regulating valve frequent jams; The ferric oxide deposition of water wall throttle orifice causes booster.Developed the feed water oxygenation treatment process for this reason; namely from the treated system outlet of condensed water and deoxygenator outlet, add oxygen; under mobile pure water condition; make steel surface form " ferric oxide+Z 250 " double shielding film of one deck even compact with appropriate oxygen, make the corrosion of therrmodynamic system carbon steel obtain effective inhibition.
Yet in recent years; whole nation thermal power plant peels off and stops up the pipe explosion accident cause and frequently occur because of oxide skin; repeatedly this class accident occurred in 1 year in some boiler; serious reaches 10 times more than; security, reliability and the economy of boiler operatiopn have greatly been affected; countless fact proved, oxygenation has accelerated the speed that steam oxidation and oxide skin come off, and this is because excessive oxygen can destroy the residing environment of " ferric oxide+Z 250 " double shielding film.The chromic oxide that is mingled with in the double shielding film and the reaction of high temperature oxygen-containing steam generate the gaseous state oxyhydroxide; the double shielding membrane interface is because chromium evaporation dissipation forms hole; hole is progressively increased and is caused double-deck oxide skin interface bond strength progressively to reduce, and finally causes catastrophic oxide skin case accident.
Therefore when carrying out the feed water oxygenation processing, how effectively to control oxygen-adding amount, the shortcoming (effectively controlling the high-temperature steam oxidation rate of heating surface) that effectively suppresses to accelerate because of oxygenation the speed that steam oxidation and oxide skin comes off when giving full play to the advantage that oxygenation processes has become the gordian technique that needs to be resolved hurrily.Developed at present directed micro-oxygenation technology, i.e. the strict oxygen amount that arrives high-temperature surface of controlling.For example, application publication number CN102603085A, the Chinese patent of Shen Qing Publication day 2012.07.25 discloses a kind of station boiler feed water oxygenation treatment process, implement under employing OT treatment process, be applicable to Once-through Boiler and drum boiler, the oxygenation stage comprises: mem stage is mended in constant oxidation conversion stage and the operation of little oxygen; The constant oxidation conversion stage is carried out oxidation for the entrance of water-supplying pump while oxygenation in condensed water precision processing system outlet and high-pressure feed water system to water feeding system, and the dissolved oxygen concentration in the control main steam≤5 μ g/L; The operation of little oxygen is mended mem stage for after forming oxide film until water feeding system, reduces the oxygen-adding amount of high-pressure feed water system, makes the oxygen that adds only for repairing with keep oxide film, controls simultaneously dissolved oxygen concentration in main steam≤5 μ g/L.its weak point is, this technique is controlled dissolved oxygen concentration in main steam≤5 μ g/L at the constant oxidation stage, namely at the constant oxidation stage, the Dissolved Oxygen concentration Control in main steam (is controlled at 50 ~ 1505 μ g/L with the oxygen-adding amount of the treated system outlet of condensed water at the steady state value of≤5 μ g/ L, simultaneously the oxygen-adding amount of the entrance of water-supplying pump of high-pressure feed water system is controlled at 50 ~ 150 μ g/L), and in the foundation of constant oxidation stage along with system ferric oxide protective membrane, can cause the oxygen amount of system consumption to descend, therefore can cause the excessive of oxygen in the constant oxidation conversion later stage in stage, make the oxygen amount of actual arrival high-temperature surface rise, in addition, the oxygen-adding amount that mem stage reduction high pressure water system is mended in little oxygen operation in this technique makes the oxygen amount only meet and repair and keep oxide film, but mend mem stage in little oxygen operation oxygen-adding amount is not had concrete regulation index, due under different operating modes, the damaged degree of oxide film is different from the state of oxidation of high-temperature surface, therefore the needed oxygen amount of water feeding system is different, so just, be easy to cause the oxygen-adding amount of high pressure water system not enough or excessive, that is to say that this technique can not really control the high-temperature steam oxidation rate of heating surface effectively.
Summary of the invention
The present invention is in order to solve the existing the problems referred to above of prior art, a kind of oiler feed oxygenation treatment process is provided, the present invention is by the monitor hydrogen amount, the strict oxygen amount that arrives high-temperature surface of controlling, can effectively control the high-temperature steam oxidation rate of heating surface, limit to greatest extent oxygenation and accelerate the shortcoming of the speed that steam oxidation and oxide skin comes off on the basis of the advantage of giving full play to oxygenation.
To achieve these goals, the present invention is by the following technical solutions:
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 35 ~ 40 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.01 ~ 0.03% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.more than 570 ℃, water molecules can be decomposed into the hydrogen-oxygen atomic structure, the iron of Sauerstoffatom meeting oxidized surface forms metal oxide film, the high-temperature steam oxidation of heating surface is more serious, in steam, the hydrogen amount is just higher, but just changed this molecular balance after oxygenation, metal is direct and oxygen reaction just, and the oxygen that adds is more, hydrogen is just fewer, therefore in stationary phase of boiler operatiopn, too much or the very few comparatively serious oxidative phenomena of boiler high temperature heating surface existence that all can illustrate of hydrogen amount, as long as control the hydrogen amount in rational scope, just can think that added oxygen does not produce larger negative effect to the high-temperature surface steam oxidation, the present invention is that the data that obtain in conjunction with actually operating again on the basis of this know-why of contriver are through design, obtain after optimization.the present invention is limited to the oxygen-adding amount of 35 ~ 40 μ g/L with strict Controlling System with condensed water precision processing system outlet and the initial oxygen-adding amount of deoxygenator outlet in first month, the contriver sums up and draws in real work, initial oxygen-adding amount is limited to 35 ~ 40 μ g/L just can set up complete " ferric oxide+Z 250 " double shielding film, cross and can not form at least whole " ferric oxide+Z 250 " double shielding film, cross and can accelerate steam oxidation at most and oxide skin comes off, and the oxygenation stage in early stage in the present invention is mainly the establishment stage of " ferric oxide+Z 250 " double shielding film on heating surface, in this stage, foundation along with system " ferric oxide+Z 250 " double shielding film, the oxygen amount of system consumption descends, therefore As time goes on, the present invention reduces the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet with 0.01 ~ 0.03% amplitude per month that (said oxygen-adding amount reduces gradually with 0.01 ~ 0.03% amplitude per month gradually here, the benchmark that reduces is the oxygen-adding amount of past month, be not take initial oxygen-adding amount as benchmark), in the excessive risk that causes acceleration steam oxidation and oxide skin to come off that guarantees when " ferric oxide+Z 250 " double shielding film is set up to reduce as far as possible because of oxygen-adding amount, more can effectively control the high-temperature steam oxidation rate of heating surface, the contriver sums up discovery in actually operating in addition, the first month in oxygenation stage at initial stage, control the condensed water precision processing system outlet and export initial oxygen-adding amount at 35 ~ 40 μ g/L with deoxygenator, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.01 ~ 0.03% amplitude per month, under this prerequisite, in boiler systems, be about 1 year the Time Created of " ferric oxide+Z 250 " double shielding film, " ferric oxide+Z 250 " double shielding film is in stabilization process afterwards, namely boiler systems is in comparatively stable system, therefore, after the contriver is set in the transformation point in oxygenation stage at initial stage and oxygenation stage in later stage feed water oxygenation and process starts according to actual condition the 12 month, be the oxygenation stage at initial stage (namely the time in oxygenation stage at initial stage is 1 year) in 12 months after namely self-water-supply oxygenation processing starts, and be the oxygenation stage in later stage after 12 months, take 12 months as transformation point, also more be conducive to the present invention in industrial actual enforcement.Owing to being mainly the forming process of " ferric oxide+Z 250 " double shielding film in the oxygenation stage in early stage; the oxidising process that has effectively suppressed high-temperature surface; make the high-temperature steam oxidation rate of boiler systems heating surface obtain actual effective control; and " ferric oxide+Z 250 " double shielding film that forms is comparatively fine and close; difficult drop-off; namely the oxygenation stage at initial stage does not have serious oxidising process and the oxide skin process that comes off, and therefore the oxygenation stage does not limit the hydrogen amount in steam in the early stage.and the oxygenation stage in later stage is mainly that oxygenation is to keep and to repair " ferric oxide+Z 250 " double shielding film, the oxygen demand reduces, therefore to reduce oxygen-adding amount, but " ferric oxide+Z 250 " double shielding membrane structure that forms due to this moment has become more unstable, therefore under different operating modes, the damaged degree of oxide film is all different from the state of oxidation of high-temperature surface, this can directly cause the variation of hydrogen content in steam, it is also different causing simultaneously the needed oxygen amount of water feeding system, therefore the present invention monitors the impact of oxygenation on the high-temperature surface oxidation by the hydrogen amount of measuring in steam, and according to the variation of the hydrogen amount in steam, regulate and control oxygen-adding amount, the monitoring of hydrogen amount is that a kind of existing routine techniques means (can be with reference to " application of ultra supercritical unit steam hydrogen content Monitoring techniques ", Zhou Jiang, Yu Mingfang), therefore at this, do not repeat.the present inventor draws after constantly groping test, the oxygen-adding amount that exports when the oxygen-adding amount of controlling the deoxygenator outlet and deoxygenator is below 30 μ g/L, simultaneously deoxygenator import hydrogen amount is stabilized in 0.2 ~ 0.4 μ g/L, when in main steam, the hydrogen amount is stabilized in 0.4 ~ 0.8 μ g/L, added oxygen can not produce larger negative effect to the high-temperature surface steam oxidation, the oxygen-adding amount that namely exports when the oxygen-adding amount of controlling the deoxygenator outlet and deoxygenator is below 30 μ g/L, deoxygenator import hydrogen amount is stabilized in 0.2 ~ 0.4 μ g/L, when in main steam, the hydrogen amount is stabilized in 0.4 ~ 0.8 μ g/L, can control to greatest extent the shortcoming of oxygenation on the basis of the advantage of giving full play to oxygenation, the present invention by the monitor hydrogen amount to adjust oxygen-adding amount, more strictly control the oxygen amount that arrives high-temperature surface, effectively control the high-temperature steam oxidation rate of heating surface, unstable due to operating mode in the present invention, can not be with stabilized hydrogen in deoxygenator import hydrogen amount and main steam a fixed value, as long as guarantee that in deoxygenator import hydrogen amount and main steam, the hydrogen amount fluctuates in above-mentioned scope.
As preferably, the first month in oxygenation stage at initial stage, control the initial oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet at 36 ~ 38 μ g/L.
As preferably, after the first month in oxygenation stage at initial stage, the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet reduces with 0.015 ~ 0.025% amplitude per month.
As preferably, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting the condensed water precision processing system import is stabilized in 0.2 ~ 0.3 μ g/L to control deoxygenator import hydrogen amount.
As preferably, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting the deoxygenator outlet is to control in main steam the hydrogen amount at 0.5 ~ 0.7 μ g/L.
Therefore, the invention has the beneficial effects as follows:
The stage of (1) oxygenation being processed is divided into oxygenation stage at initial stage and oxygenation stage in later stage, and the transformation point in oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, and so more is conducive to the present invention in industrial actual enforcement;
(2) first month in oxygenation stage at initial stage, control the condensed water precision processing system outlet and export initial oxygen-adding amount at 35 ~ 40 μ g/L with deoxygenator, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.01 ~ 0.03% amplitude per month,, in the excessive risk that causes acceleration steam oxidation and oxide skin to come off that guarantees when " ferric oxide+Z 250 " double shielding film is set up to reduce as far as possible because of oxygen-adding amount, more can effectively control the high-temperature steam oxidation rate of heating surface;
(3) in the oxygenation stage in later stage, the oxygen-adding amount of control condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount at 0.4 ~ 0.8 μ g/L, the present invention has provided concrete hydrogen richness controlling valu, by the monitor hydrogen amount and with reference to the controlling valu of hydrogen richness to adjust oxygen-adding amount, more strictly control the oxygen amount that arrives high-temperature surface, effectively control the high-temperature steam oxidation rate of heating surface, can control to greatest extent the shortcoming of oxygenation on the basis of the advantage of giving full play to oxygenation.
Embodiment
The present invention will be further described below by concrete embodiment.
In the present invention, if no special instructions, be this area ordinary method.
Embodiment 1
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 35 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.01% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 2
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 39 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.016% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 3
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 40 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.03% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 4
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 36 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.015% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.3 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
Embodiment 5
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 37 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.02% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.3 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
Embodiment 6
a kind of oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 38 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.025% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.3 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
The present invention has provided concrete hydrogen richness controlling valu, by the monitor hydrogen amount and with reference to the controlling valu of hydrogen richness to adjust oxygen-adding amount, more strictly control the oxygen amount that arrives high-temperature surface, thereby effectively control the high-temperature steam oxidation rate of heating surface.North, the Zhejiang 1000MW of logical sequence electricity generating corporation, Ltd ultra supercritical unit just adopts the present invention to carry out oxygen supply and processes operation when going into operation, so far moved 5 years left and right time, the gamma-rays inspection shows, high temperature reheater exit bend major part is not found the foreign matter accumulation, only has indivedual lower elbows that micro-foreign matter is arranged.This explanation the present invention can control the shortcoming of oxygenation to greatest extent on the basis of the advantage of giving full play to oxygenation, can prevent the booster that comes off and cause due to oxide skin, thereby guarantee security, reliability and the economy of boiler operatiopn.
Above-described embodiment is a kind of better scheme of the present invention, not the present invention is done any pro forma restriction, also has other variant and remodeling under the prerequisite that does not exceed the technical scheme that claim puts down in writing.
Claims (5)
1. oiler feed oxygenation treatment process, being included in the condensed water precision processing system outlet processes with the feed water oxygenation that the deoxygenator outlet is carried out oxygenation to water feeding system, it is characterized in that, the stage that feed water oxygenation is processed comprises oxygenation stage at initial stage and oxygenation stage in later stage, the transformation point in described oxygenation stage at initial stage and oxygenation stage in later stage is that the self-water-supply oxygenation is processed the 12 month after starting, the first month in oxygenation stage at initial stage, control the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet all at 35 ~ 40 μ g/L, afterwards the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is reduced gradually with 0.01 ~ 0.03% amplitude per month, in the oxygenation stage in later stage, the oxygen-adding amount of controlling the condensed water precision processing system outlet is below 30 μ g/L and make deoxygenator import hydrogen amount be stabilized in 0.2 ~ 0.4 μ g/L, the oxygen-adding amount of controlling simultaneously the deoxygenator outlet below 30 μ g/L and in making main steam the hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
2. a kind of oiler feed oxygenation treatment process according to claim 1, is characterized in that, the first month in oxygenation stage at initial stage is controlled the initial oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet at 36 ~ 38 μ g/L.
3. a kind of oiler feed oxygenation treatment process according to claim 1 and 2, is characterized in that, after the first month in oxygenation stage at initial stage, the oxygen-adding amount of condensed water precision processing system outlet and deoxygenator outlet is with 0.015 ~ 0.025% amplitude reduction per month.
4. a kind of oiler feed oxygenation treatment process according to claim 1, is characterized in that, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting the condensed water precision processing system import is stabilized in 0.2 ~ 0.3 μ g/L to control deoxygenator import hydrogen amount.
5. according to claim 1 or 4 described a kind of oiler feed oxygenation treatment process, is characterized in that, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting the deoxygenator outlet is to control in main steam the hydrogen amount at 0.5 ~ 0.7 μ g/L.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104328426A (en) * | 2014-09-28 | 2015-02-04 | 南阳起重机械厂有限公司 | Surface oxidation method of high-strength circular-ring chain |
| CN104326547A (en) * | 2014-10-23 | 2015-02-04 | 国家电网公司 | High-pressure water supply micro-aerobic accurate control method and high-pressure water supply micro-aerobic accurate control device for coal-fired unit boiler |
| CN113654027A (en) * | 2021-04-29 | 2021-11-16 | 西安热工研究院有限公司 | Water supply and oxygen adding treatment system and method for drum boiler under accurate oxygen adding technical condition |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5009714A (en) * | 1989-08-25 | 1991-04-23 | Halliburton Company | Process for removing copper and copper oxide deposits from surfaces |
| RU2064151C1 (en) * | 1993-08-06 | 1996-07-20 | Всероссийский теплотехнический научно-исследовательский институт | Method for cleaning and passivating working medium path of once-through boiler |
| CN101423282A (en) * | 2008-12-01 | 2009-05-06 | 河南电力试验研究院 | Station boiler and water and oxygen supply apparatus and method thereof |
| CN101851020A (en) * | 2010-04-29 | 2010-10-06 | 浙江省电力试验研究院 | DC boiler feed water selective oxidation treatment process |
| CN102603085A (en) * | 2012-03-20 | 2012-07-25 | 浙江省电力试验研究院 | Water feeding and oxygen adding process for power station boiler |
| CN102942269A (en) * | 2012-11-29 | 2013-02-27 | 淮浙煤电有限责任公司 | Concurrent boiler feed water treatment method for weak oxidation treatment and pH (potential of hydrogen) coordination control |
-
2013
- 2013-06-08 CN CN201310226836.9A patent/CN103387292B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5009714A (en) * | 1989-08-25 | 1991-04-23 | Halliburton Company | Process for removing copper and copper oxide deposits from surfaces |
| RU2064151C1 (en) * | 1993-08-06 | 1996-07-20 | Всероссийский теплотехнический научно-исследовательский институт | Method for cleaning and passivating working medium path of once-through boiler |
| CN101423282A (en) * | 2008-12-01 | 2009-05-06 | 河南电力试验研究院 | Station boiler and water and oxygen supply apparatus and method thereof |
| CN101851020A (en) * | 2010-04-29 | 2010-10-06 | 浙江省电力试验研究院 | DC boiler feed water selective oxidation treatment process |
| CN102603085A (en) * | 2012-03-20 | 2012-07-25 | 浙江省电力试验研究院 | Water feeding and oxygen adding process for power station boiler |
| CN102942269A (en) * | 2012-11-29 | 2013-02-27 | 淮浙煤电有限责任公司 | Concurrent boiler feed water treatment method for weak oxidation treatment and pH (potential of hydrogen) coordination control |
Non-Patent Citations (3)
| Title |
|---|
| 周臣等: "锅炉给水加氧处理中钝化膜性能的试验研究", 《电力建设》 * |
| 张珊敏等: "锅炉给水加氧处理的分析及应用", 《天津电力技术》 * |
| 马志国等: "直流锅炉给水加氧自动控制系统改造", 《热力发电》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104328426A (en) * | 2014-09-28 | 2015-02-04 | 南阳起重机械厂有限公司 | Surface oxidation method of high-strength circular-ring chain |
| CN104328426B (en) * | 2014-09-28 | 2017-11-24 | 南阳起重机械厂有限公司 | High-tensile round-link chain bar process for surface oxidation |
| CN104326547A (en) * | 2014-10-23 | 2015-02-04 | 国家电网公司 | High-pressure water supply micro-aerobic accurate control method and high-pressure water supply micro-aerobic accurate control device for coal-fired unit boiler |
| CN104326547B (en) * | 2014-10-23 | 2015-12-09 | 国家电网公司 | A kind of coal unit Boiler High Pressure feeds water micro-oxygen accurate control method and device |
| CN113654027A (en) * | 2021-04-29 | 2021-11-16 | 西安热工研究院有限公司 | Water supply and oxygen adding treatment system and method for drum boiler under accurate oxygen adding technical condition |
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