CN103387292B - 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 oiler feed processing technology field, especially relate to a kind of oiler feed oxygenation treatment process.
Background technology
Entirely volatilizing under the anaerobic, high pH value operating mode of processing at boiler, easily there is mobile accelerated corrosion (FAC) in feedwater, draining system, and economizer, water wall sedimentation rate are high.And produce thus a series of problem, as causing unit boiler pressure reduction, fouling rises soon; 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 feed water oxygenation treatment process for this reason; namely add oxygen from the treated system outlet of condensed water and deoxygenator outlet; under mobile pure water condition; " ferric oxide+Z 250 " double shielding film that makes steel surface formation one deck even compact with appropriate oxygen, makes the corrosion of therrmodynamic system carbon steel obtain effective inhibition.
But in recent years; whole nation thermal power plant peels off and stops up the pipe explosion accident that causes and frequently occur because of oxide skin; within 1 year, there is repeatedly this class accident in some boiler; serious reaches 10 times more than; security, reliability and the economy of boiler operatiopn are greatly 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 being mingled with in double shielding film reacts with high temperature oxygen-containing steam and generates gaseous state oxyhydroxide; 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 in the time carrying out 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 in the advantage of giving full play to oxygenation processing has become gordian technique urgently to be resolved hurrily.Develop 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, under employing OT treatment process, implement, 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 micro-oxygen; The constant oxidation conversion stage is at the entrance of water-supplying pump while of condensed water precision processing system outlet and high-pressure feed water system oxygenation, water feeding system to be oxidized, and controls the dissolved oxygen concentration≤5 μ g/L in main steam; Micro-oxygen operation is mended mem stage for after water feeding system forms oxide film, reduces the oxygen-adding amount of high-pressure feed water system, makes the oxygen adding only for repairing and maintaining oxide film, controls the dissolved oxygen concentration≤5 μ g/L in main steam simultaneously.Its weak point is, dissolved oxygen concentration≤5 μ the g/L of this technique in constant oxidation stage control main steam, namely at constant oxidation stage, the Dissolved Oxygen concentration Control in main steam (is controlled to 50 ~ 1505 μ g/L by the oxygen-adding amount of the treated system outlet of condensed water at a steady state value of≤5 μ g/ L, the oxygen-adding amount of the entrance of water-supplying pump of high-pressure feed water system is controlled to 50 ~ 150 μ g/L) simultaneously, and the foundation along with system ferric oxide protective membrane at constant oxidation stage, can cause the oxygen amount of system consumption to decline, 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 increase, in addition, the oxygen-adding amount that mem stage reduction high pressure water system is mended in micro-oxygen operation in this technique makes oxygen amount only meet and repair and maintain oxide film, but mend mem stage in micro-oxygen operation oxygen-adding amount is not had to 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 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, on the basis of advantage of giving full play to oxygenation, limit to greatest extent oxygenation and accelerate the shortcoming of the speed that steam oxidation and oxide skin comes off.
To achieve these goals, the present invention is by the following technical solutions:
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.More than 570 DEG C, water molecules can be decomposed into 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, hydrogen amount is just higher, but when just having changed this molecular balance after oxygenation, metal just directly reacts with oxygen, and the oxygen adding 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 hydrogen amount in rational scope, just can think that added oxygen does not produce larger negative effect to 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, after optimization, obtain.Condensed water precision processing system outlet and the initial oxygen-adding amount that deoxygenator exports in first month are limited to the oxygen-adding amount of 35 ~ 40 μ g/L with strict Controlling System by the present invention, 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 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, along with the foundation of system " ferric oxide+Z 250 " double shielding film, the oxygen amount of system consumption declines, 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 monthly that (said oxygen-adding amount reduces gradually with 0.01 ~ 0.03% amplitude monthly gradually here, the benchmark reducing is the oxygen-adding amount of past month, be not taking initial oxygen-adding amount as benchmark), in ensureing the foundation of " ferric oxide+Z 250 " double shielding film, reduce as far as possible the excessive risk that causes acceleration steam oxidation and oxide skin to come off because of oxygen-adding amount, more can effectively control the high-temperature steam oxidation rate of heating surface, in addition contriver sums up discovery in actually operating, the first month in oxygenation stage at initial stage, control 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 monthly, 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 contriver is set in the transformation point in oxygenation stage at initial stage and oxygenation stage in later stage feed water oxygenation processing and starts according to actual condition the 12 month, it in 12 months after namely self-water-supply oxygenation processing starts, is the oxygenation stage at initial stage (namely the time in oxygenation stage at initial stage is 1 year), and be the oxygenation stage in later stage after 12 months, taking 12 months as transformation point, also be more 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; effectively suppress the oxidising process of 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 forming 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 maintain and to repair " ferric oxide+Z 250 " double shielding film, oxygen demand reduces, therefore to reduce oxygen-adding amount, but because " ferric oxide+Z 250 " double shielding membrane structure now forming 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 the needed oxygen amount of water feeding system simultaneously, therefore the present invention monitors the impact of oxygenation on high-temperature surface oxidation by the hydrogen amount of measuring in steam, and regulate and control oxygen-adding amount according to the variation of the hydrogen amount in steam, 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 do not repeat at this.The present inventor draws after constantly groping test, when controlling the oxygen-adding amount of deoxygenator outlet and the oxygen-adding amount of deoxygenator outlet below 30 μ g/L, deoxygenator import hydrogen amount is stabilized in to 0.2 ~ 0.4 μ g/L simultaneously, when in main steam, hydrogen amount is stabilized in 0.4 ~ 0.8 μ g/L, added oxygen can not produce larger negative effect to high-temperature surface steam oxidation, namely when controlling the oxygen-adding amount of deoxygenator outlet and the oxygen-adding amount of deoxygenator outlet below 30 μ g/L, deoxygenator import hydrogen amount is stabilized in to 0.2 ~ 0.4 μ g/L, when in main steam, hydrogen amount is stabilized in 0.4 ~ 0.8 μ g/L, can on the basis of advantage of giving full play to oxygenation, control to greatest extent the shortcoming of oxygenation, the present invention by monitor hydrogen amount with 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 by stabilized hydrogen in deoxygenator import hydrogen amount and main steam a fixed value, as long as ensure that in deoxygenator import hydrogen amount and main steam, hydrogen amount fluctuates in above-mentioned scope.
As preferably, the first month in oxygenation stage at initial stage, controls condensed water precision processing system outlet and exports initial oxygen-adding amount at 36 ~ 38 μ g/L with deoxygenator.
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 monthly.
As preferably, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting 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 deoxygenator outlet is to control in main steam hydrogen amount at 0.5 ~ 0.7 μ g/L.
Therefore, the invention has the beneficial effects as follows:
(1) be divided into oxygenation stage at initial stage and oxygenation stage in later stage the stage of oxygenation processing, and the transformation point in oxygenation stage at initial stage and oxygenation stage in later stage is the 12 month after the processing of self-water-supply oxygenation starts, be so more conducive to the present invention in industrial actual enforcement;
(2) first month in oxygenation stage at initial stage, control 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 monthly, ensureing to reduce as far as possible the excessive risk that causes acceleration steam oxidation and oxide skin to come off because of oxygen-adding amount in " ferric oxide+Z 250 " double shielding film is set up, 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount at 0.4 ~ 0.8 μ g/L, the present invention has provided concrete hydrogen richness controlling valu, by 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 on the basis of advantage of giving full play to oxygenation, control to greatest extent the shortcoming of oxygenation.
Embodiment
Below by concrete embodiment, the present invention will be further described.
In the present invention, if no special instructions, be this area ordinary method.
Embodiment 1
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 2
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 3
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.4 ~ 0.8 μ g/L.
Embodiment 4
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
Embodiment 5
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
Embodiment 6
A kind of oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam hydrogen amount be stabilized in 0.5 ~ 0.7 μ g/L.
The present invention has provided concrete hydrogen richness controlling valu, by 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.The Zhejiang 1000MW of Bei Lunmou electricity generating corporation, Ltd ultra supercritical unit just adopts the present invention to carry out oxygen supply and processes operation in the time going into operation, so far moved 5 years left and right time, gamma-rays inspection shows, high temperature reheater exit bend major part is not found foreign matter accumulation, only has indivedual lower elbows to have micro-foreign matter.This explanation the present invention can control to greatest extent the shortcoming of oxygenation on the basis of advantage of giving full play to oxygenation, can prevent due to the oxide skin booster causing that comes off, thereby ensure security, reliability and the economy of boiler operatiopn.
Above-described embodiment is preferably scheme of one of the present invention, not the present invention is done to any pro forma restriction, also has other variant and remodeling under the prerequisite that does not exceed the technical scheme that claim records.
Claims (5)
1. an oiler feed oxygenation treatment process, be included in condensed water precision processing system outlet, with deoxygenator outlet, water feeding system carried out to the feed water oxygenation processing of oxygenation, it is characterized in that, the stage of feed water oxygenation processing 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 the 12 month after the processing of self-water-supply oxygenation starts, 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 monthly, in the oxygenation stage in later stage, the oxygen-adding amount of controlling 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 simultaneously controlling deoxygenator outlet below 30 μ g/L and in making main steam 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 condensed water precision processing system outlet and exported initial oxygen-adding amount at 36 ~ 38 μ g/L with deoxygenator.
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 monthly 0.015 ~ 0.025% amplitude reduction.
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 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 a kind of oiler feed oxygenation treatment process described in claim 1 or 4, it is characterized in that, in the oxygenation stage in later stage, the oxygen-adding amount of adjusting deoxygenator outlet is to control in main steam hydrogen amount at 0.5 ~ 0.7 μ g/L.
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| CN101851020B (en) * | 2010-04-29 | 2012-02-01 | 浙江省电力试验研究院 | DC boiler feed water selective oxidation treatment process |
| CN102603085B (en) * | 2012-03-20 | 2013-09-04 | 浙江省电力公司电力科学研究院 | Water feeding and oxygen adding process for power station boiler |
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