CN104089275B - Condensed water demineralized water indirect heat exchange secondary deaerating plant - Google Patents
Condensed water demineralized water indirect heat exchange secondary deaerating plant Download PDFInfo
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- CN104089275B CN104089275B CN201410261595.6A CN201410261595A CN104089275B CN 104089275 B CN104089275 B CN 104089275B CN 201410261595 A CN201410261595 A CN 201410261595A CN 104089275 B CN104089275 B CN 104089275B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 436
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000006392 deoxygenation reaction Methods 0.000 claims abstract description 68
- 238000002156 mixing Methods 0.000 claims abstract description 45
- 238000009833 condensation Methods 0.000 claims abstract description 42
- 230000005494 condensation Effects 0.000 claims abstract description 42
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 210000004907 gland Anatomy 0.000 claims abstract description 21
- 239000010865 sewage Substances 0.000 claims description 48
- 238000001816 cooling Methods 0.000 claims description 29
- 238000011033 desalting Methods 0.000 claims description 28
- 238000001354 calcination Methods 0.000 claims description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 15
- 238000010612 desalination reaction Methods 0.000 claims description 14
- 238000005070 sampling Methods 0.000 claims description 13
- 230000008676 import Effects 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 6
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 22
- 239000002585 base Substances 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 12
- 239000001301 oxygen Substances 0.000 description 12
- 229910052760 oxygen Inorganic materials 0.000 description 12
- 239000012535 impurity Substances 0.000 description 9
- 238000004880 explosion Methods 0.000 description 4
- 238000004134 energy conservation Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000003020 moisturizing effect Effects 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The present invention relates to a kind of condensed water demineralized water indirect heat exchange secondary deaerating plant, pressure-bearing surge tank is connected with first and third water inlet pipe being positioned at upper strata and second, four water inlet pipes being positioned at lower floor; Condensation by mixing water respectively by the 3rd, the 4th heat exchanger and synthetic ammonia demineralized water, convert demineralized water indirect heat exchange after access second, four water inlet pipes respectively, synthetic ammonia demineralized water and conversion demineralized water by accessing first and third water inlet pipe respectively after the 3rd, the 4th heat exchanger heat exchange; Surge tank gland steam exhauster is connected with in the middle part of the roof of pressure-bearing surge tank; Surge tank water outlet sends into higher-pressure deaerator through the first water pump, the draining of deoxygenation case sends into boiler replenishing water pipe through the 3rd water pump, the deoxygenation crown portion of higher-pressure deaerator is connected with the deoxygenation head gland steam exhauster of discharge deoxygenation exhaust steam and incoagulable gas, and pressure-bearing surge tank base plate is connected with blow-off pipe.This device condensation water residual heat utilization rate is high and reliable.
Description
Technical field
The present invention relates to a kind of condensed water demineralized water indirect heat exchange secondary deaerating plant, can be used for the recovery of the high-temperature condensation water of alkali factory production line generation and the demineralized water through heating.
Background technology
For preventing heat power equipment and corrosive pipeline thereof, and prevent incoagulable gas to be mixed into steam and reduce steam quality, must remove and be dissolved in dissolved oxygen in boiler replenishing water and other incoagulable gas, realize often through oxygen-eliminating device.According to Henry's law and Dalton's law, for the various gases be dissolved in the water, under pressure, the temperature of water is higher, and solubility is lower; Or under pressure, the partial pressure of gas is lower, and the solubility of this gas is lower.Thermal de-aeration is exactly when boiler replenishing water is heated to the saturation temperature under corresponding pressure, vapor partial pressure power will close to total pressure on the water surface, the partial pressure of various gas soluble in water is close to zero, therefore, water does not just have the ability of dissolved gas, gas soluble in water is just precipitated, thus the oxygen removed in water and other gases.Thermal deaerator comprises deoxygenation head and deoxygenation case, deoxygenation head is positioned at deoxygenation upper box part, the side wall upper part of deoxygenation head is connected with deoxygenation head water inlet pipe, the lower sidewall of deoxygenation head is connected with deoxygenation steam pipe, the top of deoxygenation head is connected with deoxygenation head gland steam exhauster, and the bottom of deoxygenation case is connected with deoxygenation case drainpipe.
In alkali factory production line, because a large amount of steam that uses can produce a lot of condensed water, as calcining furnace condensed water, fluid bed condensed water and dry ammonium condensed water etc., the temperature of condensed water after flash distillation utilizes still has 135 DEG C ~ 155 DEG C.In addition, synthetic ammonia and shift conversion step can use a large amount of demineralized waters as indirect cooling water, the temperature about 60 DEG C ~ 80 DEG C of the synthetic ammonia cooling and desalting water after heating, through the temperature about 60 DEG C ~ 95 DEG C of the conversion cooling and desalting water of heating.Because of the condensed water that produces and the temperature of cooling and desalting water higher, water quality meets again the requirement of boiler replenishing water, Ge Jian factory often by above steam condensate (SC) and cooling and desalting Water Sproading in the deoxygenation case of atmospheric type deaerator, then deliver to boiler as boiler replenishing water by deoxygenation case by water pump.
There is following weak point in above way of recycling: 1. oxygen-eliminating device is air suspended type, operating temperature about 104 DEG C, and condensed water and the mixed actual temperature of demineralized water are considerably beyond 104 DEG C, therefore overage by deoxygenation head and a large amount of kiting of flash tank be communicated with oxygen-eliminating device, can only waste a large amount of residual heat resources and water resource.2. greatly, by direct contact heat transfer, heat is difficult to reaching balance instantaneously, therefore easily produces thermal explosion in deoxygenation case, affects equipment safety operation for condensed water and the demineralized water temperature difference.3. there is contradiction in the continuity that the intermittence of boiler replenishing water and condensed water produce: when boiler not moisturizing or rate of water make-up little time, the valve opening that calcining furnace condensed water enters oxygen-eliminating device is less, and system builds the pressure, and calcining fire grate condensed water is not smooth; When a large amount of moisturizing of boiler, the valve opening that calcining furnace condensed water enters oxygen-eliminating device is large, and system back pressure reduces, and calcining furnace steam string, to oxygen-eliminating device, aggravates the discharge of waste heat.4. deoxygenation case limited volume, can not form effectively buffering between boiler unit and production unit.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, provide a kind of condensed water demineralized water indirect heat exchange secondary deaerating plant, condensation water residual heat utilization rate is high and can guarantee that the fluctuation of boiler replenishing water does not affect the normal operation with vapour unit.
For solving above technical problem, a kind of condensed water demineralized water indirect heat exchange secondary deaerating plant of the present invention, the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, fluid bed condensed water and dry ammonium condensed water enter calcining furnace condensate pipe, fluid bed condensate pipe and dry ammonium condensate pipe respectively, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe, described calcining furnace condensate pipe, fluid bed condensate pipe and dry ammonium condensate pipe access condensed water collector pipe respectively, also comprise the 3rd heat exchanger, 4th heat exchanger and the pressure-bearing surge tank closed, described pressure-bearing surge tank be circumferentially vertically connected with the first water inlet pipe, second water inlet pipe, 3rd water inlet pipe and the 4th water inlet pipe, described first water inlet pipe is relative with the mouth of pipe of the 3rd water inlet pipe and short transverse staggers mutually, described second water inlet pipe is relative with the mouth of pipe of the 4th water inlet pipe and short transverse staggers mutually, the height of described first water inlet pipe and the 3rd water inlet pipe is higher than described second water inlet pipe and the 4th water inlet pipe, the outlet of described condensed water collector pipe is connected with the 3rd heat exchanger condensation by mixing water inlet of described 3rd heat exchanger and the 4th heat exchanger condensation by mixing water inlet of the 4th heat exchanger respectively, 3rd heat exchanger condensation by mixing water out of described 3rd heat exchanger is connected with described second water inlet pipe, and the 4th heat exchanger condensation by mixing water out of described 4th heat exchanger is connected with described 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd heat exchanger synthetic ammonia demineralized water import of described 3rd heat exchanger, 3rd heat exchanger synthetic ammonia demineralized water outlet of described 3rd heat exchanger is connected with described first water inlet pipe, described conversion desalination water pipe converts demineralized water import with the 4th heat exchanger and is connected, and the 4th heat exchanger conversion demineralized water outlet of described 4th heat exchanger is connected with described 3rd water inlet pipe, be connected with surge tank gland steam exhauster in the middle part of the roof of described pressure-bearing surge tank, described surge tank gland steam exhauster is provided with non-return valve and the first control valve from lower to upper successively, the surge tank outlet pipe of opening upwards is provided with in described pressure-bearing surge tank, the lower end of described surge tank outlet pipe is connected with the entrance of the first water pump through the base plate of pressure-bearing surge tank, described first water delivery side of pump is through the deoxygenation head water inlet pipe of the 5th control valve access higher-pressure deaerator, the entrance of deoxygenation case drainpipe access the 3rd water pump of described higher-pressure deaerator, described 3rd water delivery side of pump access boiler replenishing water pipe, external steam is by the 4th control valve access deoxygenation steam pipe, the deoxygenation crown portion of described higher-pressure deaerator is connected with the deoxygenation head gland steam exhauster of discharge deoxygenation exhaust steam and incoagulable gas, the base plate of described pressure-bearing surge tank is provided with sewage draining exit, and described sewage draining exit is connected with blow-off pipe, described blow-off pipe is provided with the second control valve.
Relative to prior art, the present invention achieves following beneficial effect: (1) first calcining furnace condensed water, fluid bed condensed water and dry ammonium condensed water enter condensed water collector pipe becomes condensation by mixing water, condensation by mixing water, synthetic ammonia cooling and desalting water and conversion cooling and desalting water enter in pressure-bearing surge tank respectively, discharge from surge tank outlet pipe after mixing, send into higher-pressure deaerator by the first water pump and carry out deep deoxygenization, to meet the requirement of high-pressure boiler to oxygen content; Deoxygenation head steam mixes the incoagulable gas such as the oxygen overflowed in the deoxygenation exhaust steam and water produced and discharges from the deoxygenation head gland steam exhauster in deoxygenation crown portion.(2) pressure-bearing surge tank can bear certain pressure and water level can adjust in a big way, the contradiction between continuity that the intermittence of boiler replenishing water and condensed water produce can be made up, isolating with being formed between vapour unit and boiler replenishing water system and cushioning, guarantee that the fluctuation of boiler replenishing water does not affect the normal operation with vapour unit, avoid when boiler replenishing water amount hour, condensed water pipe network back pressure is high, and calcining furnace, fluid bed and dry ammonium system occur that the row's of building the pressure condensed water is not smooth; It also avoid when a large amount of moisturizing of boiler, condensed water pipe network back pressure is low, and the steam string of calcining furnace and fluidized system, to oxygen-eliminating device, aggravates the discharge of waste heat.(3) the temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and containing incoagulable gas such as oxygen, high and the incoagulable gas such as oxygen-free gas of condensation by mixing coolant-temperature gage, synthetic ammonia cooling and desalting water, conversion cooling and desalting water and the mixed rear temperature of condensation by mixing water rise, and the pressure-bearing surge tank operating pressure saturation pressure that to be pressure-bearing surge tank mixing water temperature corresponding, the partial pressure of oxygen and other incoagulable gas is close to zero, solubility is close to zero, discharge from pressure-bearing surge tank gland steam exhauster with surge tank exhaust steam after overflowing the pressure-bearing surge tank water surface, realize one-level deoxygenation, water through one-level deoxygenation is discharged the deoxygenation head water inlet pipe sending into higher-pressure deaerator through the first water pump and the 5th control valve by surge tank outlet pipe, external steam enters deoxygenation head from deoxygenation steam pipe and the 4th control valve and carries out secondary deoxygenation to water inlet, the incoagulable gas such as the deoxygenation exhaust steam that the mixing of deoxygenation head steam produces and oxygen are discharged from deoxygenation head gland steam exhauster, and the water through secondary deoxygenation sends into boiler as boiler replenishing water by the 3rd water pump.(4) the non-return valve on surge tank gland steam exhauster can guarantee that air can not pour in down a chimney in pressure-bearing surge tank, prevents from introducing extraneous oxygen.(5) the first control valve is by controlling the discharge capacity of surge tank exhaust steam, makes to maintain certain pressure in pressure-bearing surge tank, fully to receive the heat of condensed water and demineralized water, reduces the loss of surge tank exhaust steam discharge and heat, not only energy-conservation but also environmental protection.(6) improve boiler replenishing water temperature, reduce unit steam coal consumption.(7) the synthetic ammonia cooling and desalting water that temperature is relatively low, density is higher and conversion cooling and desalting water first water inlet pipe higher from position and the 3rd water inlet pipe enter, the second water inlet pipe that the condensation by mixing water that temperature is relatively high, density is lower is lower from position and the 4th water inlet pipe enter pressure-bearing surge tank, free convection can be formed in pressure-bearing surge tank, promote abundant heat exchange.(8) along with the increase of working time, can gather certain impurity bottom pressure-bearing surge tank, water quality can decline, and now can open the second control valve, discharges the water of water degradation, guarantee boiler replenishing water water quality from blow-off pipe.(9) the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, the dry ammonium condensed water of the fluid bed condensed water of 135 DEG C ~ 155 DEG C and 135 DEG C ~ 155 DEG C enters condensed water collector pipe first respectively and mixes, condensation by mixing water enters the 3rd heat exchanger and the 4th heat exchanger and the synthetic ammonia demineralized water of 60 DEG C ~ 80 DEG C and the conversion demineralized water of 60 DEG C ~ 95 DEG C more respectively and carries out indirect heat exchange, the temperature of condensation by mixing water reduces, the temperature of synthetic ammonia demineralized water and conversion demineralized water raises, reduce the temperature difference of condensation by mixing water and demineralized water, make the temperature field in pressure-bearing surge tank more even, avoid the generation of thermal explosion,
As preferred version of the present invention, the annular water distributor that the mouth of pipe that described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, the middle and lower part of each described annular water distributor is evenly distributed with the spray-hole of the axis jet to pressure-bearing surge tank respectively, the axis of each described spray-hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by ring pipe water outlet in the tank that arranges spray-hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extends the time of contact with water body in tank, realizes abundant heat exchange, avoid thermal explosion.
As preferred version of the present invention, the intracavity bottom of described pressure-bearing surge tank is provided with disturbance impeller, described disturbance impeller is fixedly connected on disturbance impeller axle, described disturbance impeller axle vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described disturbance impeller axle is connected with disturbance impeller drive motor; Described disturbance impeller axle departs from the axis of described pressure-bearing surge tank, and the plate inner wall of described pressure-bearing surge tank is provided with eddy current baffle plate, and described eddy current baffle plate is perpendicular to base plate and extend along base plate diametric(al).When needs blowdown, impurity often accumulates in the bottom of pressure-bearing surge tank, is difficult to discharge with current, now opens disturbance impeller and impurity can be flashed by bottom water flow rotation; If current are stable circulation state, then good not to the disturbance effect of impurity, disturbance impeller axle of the present invention departs from the axis of pressure-bearing surge tank, can avoid making current present stable circulation state; The eddy current baffle plate that plate inner wall is installed thoroughly can destroy circulation more, makes current occur turbulence state, is more conducive to disturbance and the discharge of impurity.
As preferred version of the present invention, described sewage draining exit is provided with multiple, be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different-diameter of base plate.Multiple orientation of base plate distribute more sewage draining exit, can improve contaminant removal effectiveness, reduce displacement.
As preferred version of the present invention, described inner ring sewage draining exit and outer ring sewage draining exit are respectively provided with four, and the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.Inner ring sewage draining exit and outer ring sewage draining exit staggered in a circumferential direction, centered by pressure-bearing surge tank axis, be equipped with sewage draining exit to extraradial eight directions, blowdown can be made more evenly rationally, better effects if, within the shortest time, get rid of as far as possible many dirts, reduce displacement.
As preferred version of the present invention, the intracavity bottom of described pressure-bearing surge tank is provided with sampling pipe, it is outer and be connected with sampling cooler that described sampling pipe stretches out pressure-bearing surge tank, the export pipeline of described sampling cooler is provided with online electric conductivity detector and online Ph value detector.In-tank mixing electrical conductivity of water and Ph value can be detected in real time.
As preferred version of the present invention, the holding wire of described online electric conductivity detector and online Ph value detector accesses the corresponding signal input of PLC respectively, and the corresponding signal output of described PLC is connected with the control line of described second control valve; When PLC detects that the Ph value that electrical conductivity that online electric conductivity detector provides is greater than setting value or online Ph value detector and provides controls the second control valve when exceeding setting range and opens, control the second control valve closedown when PLC detects that electrical conductivity that online electric conductivity detector provides is less than setting value and the Ph value that provides of Ph value detector is in setting range online.The electrical conductivity that PLC can provide according to online electric conductivity detector and the Ph value that online Ph value detector provides, the keying of automatic control disturbance impeller and the second control valve, improves the automatization level of system.
As preferred version of the present invention, described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are separately installed with temperature sensor and flowmeter, different azimuth and the differing heights of the liquid Space of described pressure-bearing surge tank are provided with multiple temperature sensor altogether, and the gas-phase space of described pressure-bearing surge tank is provided with pressure sensor.Temperature sensor can detect the water temperature of each water inlet pipe and pressure-bearing surge tank, and flowmeter can measure the actual flow of each water inlet pipe.
As preferred version of the present invention, the holding wire of described pressure sensor, each described temperature sensor and each described flowmeter accesses the corresponding signal input of PLC respectively, and the corresponding signal output of described PLC is connected with the control line of described first control valve; The aperture controlling the first control valve when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is described pressure-bearing surge tank liquid Space survey the mean value of water temperature, the force value that p surveys for described pressure sensor; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the temperature sensor on first, second, third and fourth water inlet pipe detects, and m1, m2, m3 and m4 are respectively the flow measured by the flowmeter on first, second, third and fourth water inlet pipe; P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.The set temperature value of PLC gets the weighted average water temperature t0 of each water inlet pipe, there is one-to-one relationship in the saturation pressure p0 of water vapour and water temperature t0, when temperature in tank is greater than that in design temperature or tank, pressure is greater than setting pressure, the aperture that PLC controls the first control valve strengthens, to strengthen the discharge of surge tank exhaust steam; When temperature in tank is lower than when in design temperature or tank, pressure is lower than setting pressure, the aperture that PLC controls the first control valve reduces, and prevents that steam discharge is excessive even occurs that tank outer air is poured in down a chimney; Adopt PLC automatically to regulate the aperture of the first control valve according to water temperature and pressure, improve the automatization level of system, avoid the excess emitters of surge tank exhaust steam, under guaranteeing that pressure-bearing surge tank is operated in the maximum pressure/temperature of permission, not only energy-conservation but also environmental protection.
As preferred version of the present invention, the inlet duct of described 3rd heat exchanger condensation by mixing water inlet is provided with the 7th control valve, the inlet duct of described 4th heat exchanger condensation by mixing water inlet is provided with the 8th control valve, the corresponding signal output of described PLC is connected with the control line of the 8th control valve with described 7th control valve, and described PLC controls the aperture of described 7th control valve according to the water temperature that the temperature sensor on described first water inlet pipe and the second water inlet pipe detects; Described PLC controls the aperture of described 8th control valve according to the water temperature that the temperature sensor on described 3rd water inlet pipe and the 4th water inlet pipe detects.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, and accompanying drawing only provides reference and explanation use, is not used to limit the present invention.
Fig. 1 is the schematic diagram of condensed water demineralized water indirect heat exchange secondary deaerating plant of the present invention.
Fig. 2 is the partial sectional view at pressure-bearing surge tank the 3rd water inlet pipe position in the present invention.
Fig. 3 is the base plate top view of pressure-bearing surge tank in the present invention.
In figure: PLC.PLC controller;
E1. pressure-bearing surge tank; E1a. sewage draining exit; E1b. eddy current baffle plate; E1d. disturbance impeller; E1e. sampling pipe;
G1. the first water inlet pipe; G2. the second water inlet pipe; G3. the 3rd water inlet pipe; G4. the 4th water inlet pipe; G5. surge tank gland steam exhauster; G6. surge tank outlet pipe; G7. blow-off pipe; Vd. non-return valve; V1. the first control valve; B1. the first water pump; T1. the first temperature sensor; T2. the second temperature sensor; T3. three-temperature sensor; T4. the 4th temperature sensor; T5. the 5th temperature sensor; T6. the 6th temperature sensor; T7. the 7th temperature sensor; T8. the 8th temperature sensor; P. pressure sensor; V2. the second control valve; M1. first-class gauge; M2. second gauge; M3. the 3rd flowmeter; M4. the 4th flowmeter;
Q. to sample cooler; Q1. online electric conductivity detector; Q2. online Ph value detector;
S1. calcining furnace condensate pipe; S2. fluid bed condensate pipe; S3. dry ammonium condensate pipe; S4. other condensate pipe; S0. condensed water collector pipe; Y1. synthetic ammonia desalination water pipe; Y2. desalination water pipe is converted;
E3. higher-pressure deaerator; E3a. deoxygenation steam pipe; E3b. deoxygenation head water inlet pipe; E3c. deoxygenation head gland steam exhauster; E3d. deoxygenation case drainpipe; B3. the 3rd water pump; V4. the 4th control valve; V5. the 5th control valve;
H3. the 3rd heat exchanger; H3a. the 3rd heat exchanger synthetic ammonia demineralized water import; H3b. the 3rd heat exchanger synthetic ammonia demineralized water outlet; H3c. the 3rd heat exchanger condensation by mixing water inlet; H3d. the 3rd heat exchanger condensation by mixing water out; V7. the 7th control valve;
H4. the 4th heat exchanger; H4a. the 4th heat exchanger conversion demineralized water import; H4b. the 4th heat exchanger conversion demineralized water outlet; H4c. the 4th heat exchanger condensation by mixing water inlet; H4d. the 4th heat exchanger condensation by mixing water out; V8. the 8th control valve.
Detailed description of the invention
As shown in Figure 1, condensed water demineralized water indirect heat exchange secondary deaerating plant of the present invention, comprises closed pressure-bearing surge tank E1, the 3rd heat exchanger H3 and the 4th heat exchanger H4.The calcining furnace condensed water of 135 DEG C ~ 155 DEG C enters calcining furnace condensate pipe S1, the fluid bed condensed water of 135 DEG C ~ 155 DEG C enters fluid bed condensate pipe S2, the dry ammonium condensed water of 135 DEG C ~ 155 DEG C enters dry ammonium condensate pipe, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe Y1, the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe Y2, calcining furnace condensate pipe S1, fluid bed condensate pipe S2 and dry ammonium condensate pipe S3 access condensed water collector pipe S0 respectively, also other condensate pipe S4 can be accessed condensed water collector pipe S0.
Pressure-bearing surge tank E1 is circumferentially vertically connected with the first water inlet pipe G1, the second water inlet pipe G2, the 3rd water inlet pipe G3 and the 4th water inlet pipe G4, first water inlet pipe G1 is relative with the mouth of pipe of the 3rd water inlet pipe G3 and short transverse staggers mutually, second water inlet pipe G2 is relative with the mouth of pipe of the 4th water inlet pipe G4 and short transverse staggers mutually, and the height of the first water inlet pipe G1 and the 3rd water inlet pipe G3 is higher than the second water inlet pipe G2 and the 4th water inlet pipe G4.Access the first water inlet pipe G1 and the 3rd water inlet pipe G3 respectively after synthetic ammonia cooling and desalting water and conversion cooling and desalting water heat up, after condensation by mixing water for cooling, access the second water inlet pipe G2 and the 4th water inlet pipe G4 respectively, be connected with surge tank gland steam exhauster G5 in the middle part of the roof of pressure-bearing surge tank E1, surge tank gland steam exhauster G5 be provided with from lower to upper successively non-return valve Vd and the first control valve V1, the surge tank outlet pipe G6 of opening upwards is provided with in pressure-bearing surge tank E1, the lower end of surge tank outlet pipe G6 is connected with the entrance of the first water pump B1 through the base plate of pressure-bearing surge tank E1, the outlet of the first water pump B1 accesses the deoxygenation head water inlet pipe E3b of higher-pressure deaerator E3 through the 5th control valve V5, the deoxygenation case drainpipe E3d of higher-pressure deaerator E3 accesses the entrance of the 3rd water pump B3, the outlet access boiler replenishing water pipe of the 3rd water pump B3, external steam accesses deoxygenation steam pipe E3a by the 4th control valve V4, the deoxygenation crown portion of higher-pressure deaerator E3 is connected with the deoxygenation head gland steam exhauster E3c of discharge deoxygenation exhaust steam and incoagulable gas.
The base plate of pressure-bearing surge tank E1 is provided with sewage draining exit E1a, and sewage draining exit E1a is connected with blow-off pipe G7, blow-off pipe G7 is provided with the second control valve V2.
The outlet of condensed water collector pipe S0 is connected with the 3rd heat exchanger condensation by mixing water inlet H3c of the 3rd heat exchanger H3 and the 4th heat exchanger condensation by mixing water inlet H4c of the 4th heat exchanger H4 respectively, the 3rd heat exchanger condensation by mixing water out H3d of the 3rd heat exchanger H3 is connected with the second water inlet pipe G2, and the 4th heat exchanger condensation by mixing water out H4d of the 4th heat exchanger H4 is connected with the 4th water inlet pipe G4; Synthetic ammonia desalination water pipe Y1 is connected with the 3rd heat exchanger synthetic ammonia demineralized water import H3a of the 3rd heat exchanger H3, the 3rd heat exchanger synthetic ammonia demineralized water outlet H3b of the 3rd heat exchanger H3 is connected with the first water inlet pipe G1, conversion desalination water pipe Y2 converts demineralized water import H4a with the 4th heat exchanger and is connected, and the 4th heat exchanger conversion demineralized water outlet H4b of the 4th heat exchanger H4 is connected with the 3rd water inlet pipe G3.
During work, the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, the dry ammonium condensed water of the fluid bed condensed water of 135 DEG C ~ 155 DEG C and 135 DEG C ~ 155 DEG C enters condensed water collector pipe S0 first respectively and mixes, other condensed water also can enter condensed water collector pipe S0 and mix, condensation by mixing water enters the 3rd heat exchanger H3 and the 4th heat exchanger H4 and the 60 DEG C ~ synthetic ammonia demineralized water of 80 DEG C more respectively and the conversion demineralized water of 60 DEG C ~ 95 DEG C carries out indirect heat exchange, the temperature of condensation by mixing water reduces, the temperature of synthetic ammonia demineralized water and conversion demineralized water raises, reduce the temperature difference of condensation by mixing water and demineralized water, make the temperature field in pressure-bearing surge tank more even.The synthetic ammonia cooling and desalting water that temperature is relatively low, density is higher and higher from position respectively the first water inlet pipe G1 of conversion cooling and desalting water and the 3rd water inlet pipe G3 enter; The second water inlet pipe G2 that the condensation by mixing water that temperature is relatively high, density is lower is lower from position and the 4th water inlet pipe G4 enters pressure-bearing surge tank E1, can form free convection, promote abundant heat exchange in pressure-bearing surge tank.Discharge from surge tank outlet pipe G6 after synthetic ammonia cooling and desalting water, conversion cooling and desalting water and condensation by mixing water are mixed, send into higher-pressure deaerator E3 by the first water pump B1 and carry out secondary deoxygenation.The temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and containing incoagulable gas such as oxygen, high and the incoagulable gas such as oxygen-free gas of condensation by mixing coolant-temperature gage, synthetic ammonia cooling and desalting water, conversion cooling and desalting water and the mixed rear temperature of condensation by mixing water rise, and the saturation pressure of the operating pressure of pressure-bearing surge tank E1 corresponding to pressure-bearing surge tank mixing water temperature, the partial pressure of oxygen and other incoagulable gas is close to zero, solubility is close to zero, discharge from surge tank gland steam exhauster G5 with surge tank exhaust steam after overflowing the pressure-bearing surge tank water surface, realize one-level deoxygenation, water through one-level deoxygenation is discharged the deoxygenation head water inlet pipe E3b sending into higher-pressure deaerator E3 through the first water pump B1 and the 5th control valve V5 by surge tank outlet pipe G6, external steam enters deoxygenation head from deoxygenation steam pipe E3a and the 4th control valve V4 and carries out secondary deoxygenation to water inlet, the incoagulable gas such as deoxygenation exhaust steam and oxygen are discharged from deoxygenation head gland steam exhauster E3c, water through secondary deoxygenation is discharged from deoxygenation case drainpipe E3d, sends into boiler as boiler replenishing water by the 3rd water pump B3.Non-return valve Vd on surge tank gland steam exhauster G5 can guarantee that air can not pour in down a chimney in pressure-bearing surge tank E1, prevents from introducing extraneous oxygen.First control valve V1 can control the discharge capacity of surge tank exhaust steam, make to maintain certain pressure in pressure-bearing surge tank E1, fully to receive the heat of condensed water and demineralized water, reduce the loss of surge tank exhaust steam discharge and heat, improve boiler replenishing water temperature, reduce unit steam coal consumption.Along with the increase of working time, can gather certain impurity bottom pressure-bearing surge tank E1, water quality can decline, and now can open the second control valve V2, from the water that blow-off pipe G7 discharges water degradation, guarantees boiler replenishing water water quality.
As improvement, first water inlet pipe G1 is provided with the first temperature sensor T1 and first-class gauge M1, second water inlet pipe G2 is provided with the second temperature sensor T2 and second gauge M2,3rd water inlet pipe G3 is provided with three-temperature sensor T3 and the 3rd flowmeter M3, the 4th water inlet pipe G4 is provided with the 4th temperature sensor T4 and the 4th flowmeter M4.Different azimuth and the differing heights of the liquid Space of pressure-bearing surge tank E1 are provided with multiple temperature sensor altogether, such as, be separately installed with the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor T8 at height different parts.The gas-phase space of pressure-bearing surge tank E1 is also provided with pressure sensor P.
For improving the automatization level of system, the holding wire of the first temperature sensor T1, the second temperature sensor T2, three-temperature sensor T3, the 4th temperature sensor T4, the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7, the 8th temperature sensor T8, first-class gauge M1, second gauge M2, the 3rd flowmeter M3, the 4th flowmeter M4 and pressure sensor P accesses the corresponding signal input of PLC respectively, and the corresponding signal output of PLC is connected with the control line of the first control valve V1.
The aperture controlling the first control valve V1 when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve V1 when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is pressure-bearing surge tank liquid Space survey the mean value of water temperature, such as the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor T8 survey the mean value of water temperature; The force value that p surveys for pressure sensor P; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the first temperature sensor T1, the second temperature sensor T2, three-temperature sensor T3 and the 4th temperature sensor T4 detect, and m1, m2, m3 and m4 are respectively first-class gauge M1, second gauge M2, the 3rd flowmeter M3 and the flow measured by the 4th flowmeter M4.P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
The set temperature value of PLC gets the weighted average water temperature t0 of each water inlet pipe, there is one-to-one relationship in the saturation pressure p0 of water vapour and water temperature t0, when temperature in tank is greater than that in design temperature or tank, pressure is greater than setting pressure, the aperture that PLC controls the first control valve V1 strengthens, to strengthen the discharge of surge tank exhaust steam; When temperature in tank is lower than when in design temperature or tank, pressure is lower than setting pressure, the aperture that PLC controls the first control valve V1 reduces, and prevents that steam discharge is excessive even occurs that tank outer air is poured in down a chimney.Adopt PLC automatically to regulate the aperture of the first control valve V1 according to water temperature and pressure, improve the automatization level of system, avoid the excess emitters of surge tank exhaust steam, under guaranteeing that pressure-bearing surge tank is operated in the maximum pressure/temperature of permission, not only energy-conservation but also environmental protection.
For improving automatization level, the inlet duct of the 3rd heat exchanger condensation by mixing water inlet H3c is provided with the 7th control valve V7, the inlet duct of the 4th heat exchanger condensation by mixing water inlet H4c is provided with the 8th control valve V8, the corresponding signal output of PLC is connected with the control line of the 8th control valve V8 with the 7th control valve V7, and PLC controls the aperture of the 7th control valve V7 according to the water temperature that the first temperature sensor T1 on the first water inlet pipe and the second temperature sensor T2 on the second water inlet pipe detects; PLC controls the aperture of the 8th control valve V8 according to the water temperature that the three-temperature sensor T3 on the 3rd water inlet pipe and the 4th temperature sensor T4 on the 4th water inlet pipe detects.
The intracavity bottom of pressure-bearing surge tank E1 can be provided with sampling pipe E1e, it is outer and be connected with sampling cooler Q that sampling pipe E1e stretches out pressure-bearing surge tank E1, the export pipeline of sampling cooler Q is provided with online electric conductivity detector Q1 and online Ph value detector Q2, to detect in-tank mixing electrical conductivity of water and Ph value in real time.
For improving the automatization level of system, the holding wire of online electric conductivity detector Q1 and online Ph value detector Q2 accesses the corresponding signal input of PLC respectively, and the corresponding signal output of PLC is connected with the control line of the second control valve V2; When PLC detects that the Ph value that electrical conductivity that online electric conductivity detector Q1 provides is greater than setting value or online Ph value detector Q2 and provides controls the second control valve V2 when exceeding setting range and opens, when PLC detect electrical conductivity that online electric conductivity detector Q1 provides be less than setting value and the Ph value that provides of online Ph value detector Q2 in setting range time control the second control valve V2 and close, realize the Ph value that the electrical conductivity that provides according to online electric conductivity detector Q1 and online Ph value detector Q2 provide, the keying of automatic control the second control valve V2.
As shown in Figure 2, as improvement, the annular water distributor that the mouth of pipe that first water inlet pipe G1, the second water inlet pipe G2, the 3rd water inlet pipe G3 and the 4th water inlet pipe G4 are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, for the 3rd water inlet pipe G3 in Fig. 2, the middle and lower part of each annular water distributor is evenly distributed with the spray-hole of the axis jet to pressure-bearing surge tank respectively, the axis of each spray-hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by ring pipe water outlet in the tank that arranges spray-hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extends the time of contact with water body in tank, realizes abundant heat exchange, avoid thermal explosion.
Because accumulation of impurities is in the bottom of pressure-bearing surge tank, be difficult to during blowdown discharge with current, at the intracavity bottom of pressure-bearing surge tank, disturbance impeller E1d can be installed, disturbance impeller E1d is fixedly connected on disturbance impeller axle, disturbance impeller axle vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of disturbance impeller axle is connected with disturbance impeller drive motor, opens disturbance impeller E1d and impurity can be flashed by bottom water flow rotation, be beneficial to discharge.
Disturbance impeller axle preferably departs from the axis of pressure-bearing surge tank, to avoid making current present stable circulation state.
As shown in Figure 3, as improvement, the plate inner wall of pressure-bearing surge tank can be provided with eddy current baffle plate E1b, eddy current baffle plate E1b is perpendicular to base plate and extend along base plate diametric(al), eddy current baffle plate E1b thoroughly can destroy circulation, makes current occur turbulence state, is more conducive to disturbance and the discharge of impurity.
Sewage draining exit E1a can be provided with multiple, such as be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different-diameter of pressure-bearing surge tank base plate.
Inner ring sewage draining exit and outer ring sewage draining exit are preferably respectively provided with four, inner ring sewage draining exit and outer ring sewage draining exit staggered in a circumferential direction, phase place staggers successively 45 ° and arrange, four inner ring sewage draining exits assume diamond in shape layout, four outer ring sewage draining exits are arranged in squares, and the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.
The foregoing is only the better possible embodiments of the present invention, non-ly therefore limit to scope of patent protection of the present invention.In addition to the implementation, the present invention can also have other embodiments.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop in the protection domain of application claims.
Claims (10)
1. a condensed water demineralized water indirect heat exchange secondary deaerating plant, the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, fluid bed condensed water and dry ammonium condensed water enter calcining furnace condensate pipe, fluid bed condensate pipe and dry ammonium condensate pipe respectively, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe, described calcining furnace condensate pipe, fluid bed condensate pipe and dry ammonium condensate pipe access condensed water collector pipe respectively, it is characterized in that: also comprise the 3rd heat exchanger, 4th heat exchanger and the pressure-bearing surge tank closed, described pressure-bearing surge tank be circumferentially vertically connected with the first water inlet pipe, second water inlet pipe, 3rd water inlet pipe and the 4th water inlet pipe, described first water inlet pipe is relative with the mouth of pipe of the 3rd water inlet pipe and short transverse staggers mutually, described second water inlet pipe is relative with the mouth of pipe of the 4th water inlet pipe and short transverse staggers mutually, the height of described first water inlet pipe and the 3rd water inlet pipe is higher than described second water inlet pipe and the 4th water inlet pipe, the outlet of described condensed water collector pipe is connected with the 3rd heat exchanger condensation by mixing water inlet of described 3rd heat exchanger and the 4th heat exchanger condensation by mixing water inlet of the 4th heat exchanger respectively, 3rd heat exchanger condensation by mixing water out of described 3rd heat exchanger is connected with described second water inlet pipe, and the 4th heat exchanger condensation by mixing water out of described 4th heat exchanger is connected with described 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd heat exchanger synthetic ammonia demineralized water import of described 3rd heat exchanger, 3rd heat exchanger synthetic ammonia demineralized water outlet of described 3rd heat exchanger is connected with described first water inlet pipe, described conversion desalination water pipe converts demineralized water import with the 4th heat exchanger and is connected, and the 4th heat exchanger conversion demineralized water outlet of described 4th heat exchanger is connected with described 3rd water inlet pipe, be connected with surge tank gland steam exhauster in the middle part of the roof of described pressure-bearing surge tank, described surge tank gland steam exhauster is provided with non-return valve and the first control valve from lower to upper successively, the surge tank outlet pipe of opening upwards is provided with in described pressure-bearing surge tank, the lower end of described surge tank outlet pipe is connected with the entrance of the first water pump through the base plate of pressure-bearing surge tank, described first water delivery side of pump is through the deoxygenation head water inlet pipe of the 5th control valve access higher-pressure deaerator, the entrance of deoxygenation case drainpipe access the 3rd water pump of described higher-pressure deaerator, described 3rd water delivery side of pump access boiler replenishing water pipe, external steam is by the 4th control valve access deoxygenation steam pipe, the deoxygenation crown portion of described higher-pressure deaerator is connected with the deoxygenation head gland steam exhauster of discharge deoxygenation exhaust steam and incoagulable gas, the base plate of described pressure-bearing surge tank is provided with sewage draining exit, and described sewage draining exit is connected with blow-off pipe, described blow-off pipe is provided with the second control valve.
2. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 1, it is characterized in that: the annular water distributor that the mouth of pipe that described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, the middle and lower part of each described annular water distributor is evenly distributed with the spray-hole of the axis jet to pressure-bearing surge tank respectively, the axis of each described spray-hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.
3. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 1, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with disturbance impeller, described disturbance impeller is fixedly connected on disturbance impeller axle, described disturbance impeller axle vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described disturbance impeller axle is connected with disturbance impeller drive motor; Described disturbance impeller axle departs from the axis of described pressure-bearing surge tank, and the plate inner wall of described pressure-bearing surge tank is provided with eddy current baffle plate, and described eddy current baffle plate is perpendicular to base plate and extend along base plate diametric(al).
4. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 1, it is characterized in that: described sewage draining exit is provided with multiple, be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different-diameter of base plate.
5. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 4, it is characterized in that: described inner ring sewage draining exit and outer ring sewage draining exit are respectively provided with four, the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.
6. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 1, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with sampling pipe, it is outer and be connected with sampling cooler that described sampling pipe stretches out pressure-bearing surge tank, the export pipeline of described sampling cooler is provided with online electric conductivity detector and on-line pH value detector.
7. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 6, it is characterized in that: the holding wire of described online electric conductivity detector and on-line pH value detector accesses the corresponding signal input of PLC respectively, the corresponding signal output of described PLC is connected with the control line of described second control valve; When PLC detects that the pH value that electrical conductivity that online electric conductivity detector provides is greater than setting value or on-line pH value detector and provides controls the second control valve when exceeding setting range and opens, when PLC detect electrical conductivity that online electric conductivity detector provides be less than setting value and the pH value that provides of on-line pH value detector in setting range time control the second control valve and close.
8. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 1, it is characterized in that: described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are separately installed with temperature sensor and flowmeter, different azimuth and the differing heights of the liquid Space of described pressure-bearing surge tank are provided with multiple temperature sensor altogether, and the gas-phase space of described pressure-bearing surge tank is provided with pressure sensor.
9. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 8, it is characterized in that: the holding wire of described pressure sensor, each described temperature sensor and each described flowmeter accesses the corresponding signal input of PLC respectively, and the corresponding signal output of described PLC is connected with the control line of described first control valve; The aperture controlling the first control valve when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is described pressure-bearing surge tank liquid Space survey the mean value of water temperature, the force value that p surveys for described pressure sensor; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the temperature sensor on first, second, third and fourth water inlet pipe detects, and m1, m2, m3 and m4 are respectively the flow measured by the flowmeter on first, second, third and fourth water inlet pipe; P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
10. condensed water demineralized water indirect heat exchange secondary deaerating plant according to claim 9, it is characterized in that: the inlet duct of described 3rd heat exchanger condensation by mixing water inlet is provided with the 7th control valve, the inlet duct of described 4th heat exchanger condensation by mixing water inlet is provided with the 8th control valve, the corresponding signal output of described PLC is connected with the control line of the 8th control valve with described 7th control valve, described PLC controls the aperture of described 7th control valve according to the water temperature that the temperature sensor on described first water inlet pipe and the second water inlet pipe detects, described PLC controls the aperture of described 8th control valve according to the water temperature that the temperature sensor on described 3rd water inlet pipe and the 4th water inlet pipe detects.
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| HUT35811A (en) * | 1983-07-18 | 1985-07-29 | Vegyterv Vegyimueveket Tervezo | Method and apparatus for thermal degassing feed-water |
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| CN201401778Y (en) * | 2009-04-23 | 2010-02-10 | 东营华泰热力有限责任公司 | Thermoelectric exhaust steam recovery unit |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| HUT35811A (en) * | 1983-07-18 | 1985-07-29 | Vegyterv Vegyimueveket Tervezo | Method and apparatus for thermal degassing feed-water |
| CN101575107A (en) * | 2008-05-08 | 2009-11-11 | 沈阳铝镁设计研究院 | Respective self-evaporation technology of new steam condensate and secondary steam condensate |
| CN201401778Y (en) * | 2009-04-23 | 2010-02-10 | 东营华泰热力有限责任公司 | Thermoelectric exhaust steam recovery unit |
| CN203068483U (en) * | 2012-12-31 | 2013-07-17 | 北京富士特锅炉有限公司 | Atmospheric waste heat recovery thermal oxygen-removing device |
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