CN104089273A - Buffer tank for mixed recovery of condensate water and desalted water as well as deoxidized exhaust steam condensing device - Google Patents
Buffer tank for mixed recovery of condensate water and desalted water as well as deoxidized exhaust steam condensing device Download PDFInfo
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- CN104089273A CN104089273A CN201410261516.1A CN201410261516A CN104089273A CN 104089273 A CN104089273 A CN 104089273A CN 201410261516 A CN201410261516 A CN 201410261516A CN 104089273 A CN104089273 A CN 104089273A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 426
- 238000011084 recovery Methods 0.000 title claims abstract description 17
- 239000000498 cooling water Substances 0.000 claims abstract description 44
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000001354 calcination Methods 0.000 claims abstract description 23
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000006392 deoxygenation reaction Methods 0.000 claims description 119
- 239000010865 sewage Substances 0.000 claims description 48
- 238000001816 cooling Methods 0.000 claims description 39
- 238000011033 desalting Methods 0.000 claims description 35
- 238000002156 mixing Methods 0.000 claims description 31
- 238000009833 condensation Methods 0.000 claims description 24
- 230000005494 condensation Effects 0.000 claims description 24
- 210000004907 gland Anatomy 0.000 claims description 23
- 239000012530 fluid Substances 0.000 claims description 16
- 238000005070 sampling Methods 0.000 claims description 14
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 12
- 230000008676 import Effects 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 6
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 47
- 230000015572 biosynthetic process Effects 0.000 abstract description 4
- 239000002918 waste heat Substances 0.000 abstract description 3
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- 239000002585 base Substances 0.000 description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 17
- 239000001301 oxygen Substances 0.000 description 17
- 229910052760 oxygen Inorganic materials 0.000 description 17
- 239000012535 impurity Substances 0.000 description 9
- 238000007599 discharging Methods 0.000 description 6
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000004134 energy conservation Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000004880 explosion Methods 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
- 238000007664 blowing Methods 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 239000000356 contaminant 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
- 238000002955 isolation Methods 0.000 description 1
- 239000000203 mixture Substances 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
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Abstract
The invention relates to a buffer tank for mixed recovery of condensate water and desalted water as well as a deoxidized exhaust steam condensing device. A first water inlet pipe, a second water inlet pipe, a third water inlet pipe and a fourth water inlet pipe are connected onto a pressure-bearing buffer tank, wherein the first water inlet pipe and the third water inlet pipe are located on the upper layer, and the second water inlet pipe and the fourth water inlet pipe are located on the lower layer; synthesis ammonia cooled desalted water and conversion cooled desalted water are introduced into the first water inlet pipe and the third water inlet pipe respectively, and calcining furnace condensate water and fluidized bed condensate water are introduced into the second water inlet pipe and the fourth water inlet pipe respectively; buffer tank exhaust steam enters a first heat exchanger and is cooled into buffer tank exhaust steam condensate water by circulating cooling water, the buffer tank exhaust steam condensate water enters a condensate water collecting tank, non-condensable gas is discharged, and the buffer tank exhaust steam condensate water is injected into the pressure-bearing tank by a second water pump; outlet water of the pressure-bearing buffer tank is sent into a high-pressure deaerator by a first water pump, drained water of a deaerator tank is sent to a boiler water replenishing pipe by a third water pump; the deoxidized exhaust steam is condensed into deoxidized exhaust steam condensate water by a second heat exchanger, and the deoxidized exhaust steam condensate water enters a condensate water collecting tank; and drain outlets are formed in a bottom plate of the pressure-bearing buffer tank. According to the device, the utilization rate of condensate water waste heat is high, and the operation is reliable.
Description
Technical field
The present invention relates to a kind of condensed water demineralized water and mix recovery surge tank and deoxygenation exhaust steam condensing unit, 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 from sneaking into steam and reduce steam quality, must remove the dissolved oxygen and other incoagulable gas that are dissolved in boiler replenishing water, often realizing by oxygen-eliminating device.According to Henry's law and Dalton's law, for the various gases that are dissolved in the water, under certain pressure, the temperature of water is higher, and solubility is lower; Or under certain 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 be close to total pressure on the water surface, the partial pressure of various gases 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, thereby removes oxygen and other gases in water.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 a deoxygenation water inlet pipe, the lower sidewall of deoxygenation head is connected with deoxygenation steam pipe, the top of deoxygenation head is connected with a deoxygenation 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 waters, as calcining furnace condensed water, fluid bed condensed water and dry ammonium condensed water etc., the temperature of condensed water after flash distillation utilization 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, approximately 60 DEG C ~ 80 DEG C of the temperature of the synthetic ammonia cooling and desalting water after heating, approximately 60 DEG C ~ 95 DEG C of the temperature of the conversion cooling and desalting water through heating.Because of the condensed water and the temperature of cooling and desalting water that produce higher, water quality meets again the requirement of boiler replenishing water, Ge Jian factory is often recycled to above steam condensate (SC) and cooling and desalting water in the deoxygenation case of atmospheric type deaerator, then delivers 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, approximately 104 DEG C of operating temperatures, and the mixed actual temperature of condensed water and demineralized water is considerably beyond 104 DEG C, therefore a large amount of kitings of flash tank that overage can only be communicated with by deoxygenation head with oxygen-eliminating device, waste a large amount of residual heat resources and water resource.2. condensed water and the demineralized water temperature difference are large, and by direct contact heat transfer, heat is difficult to reach balance in moment, therefore easily produce thermal explosion in deoxygenation case, affect equipment safety operation.3. there is contradiction in the continuity that the intermittence of boiler replenishing water and condensed water produce: when not moisturizing of boiler or rate of water make-up are when little, 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; In the time of 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 volume is limited, can not between boiler unit and production unit, form effectively buffering.
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 to mix and reclaim surge tank and deoxygenation exhaust steam condensing unit, 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 of the present invention mixes recovery surge tank and deoxygenation exhaust steam condensing unit, comprise the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, the fluid bed condensed water of 135 DEG C ~ 155 DEG C, the conversion cooling and desalting water of the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and 60 DEG C ~ 95 DEG C, also comprise the pressure-bearing surge tank of sealing, on the circumference of described pressure-bearing surge tank, be vertically connected with the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, in the relative and short transverse of the mouth of pipe of described the first water inlet pipe and the 3rd water inlet pipe, mutually stagger, in the relative and short transverse of the mouth of pipe of described the second water inlet pipe and the 4th water inlet pipe, mutually stagger, the height of described the first water inlet pipe and the 3rd water inlet pipe is higher than described the second water inlet pipe and the 4th water inlet pipe, described synthetic ammonia cooling and desalting water and conversion cooling and desalting water access respectively described the first water inlet pipe and the 3rd water inlet pipe, and described calcining furnace condensed water and fluid bed condensed water access respectively described the second water inlet pipe and the 4th water inlet pipe, the roof middle part of described pressure-bearing surge tank is connected with surge tank gland steam exhauster, and non-return valve and the first control valve are installed on described surge tank gland steam exhauster from lower to upper successively, the outlet of described the first control valve is connected with the First Heat Exchanger surge tank exhaust steam import of First Heat Exchanger, the First Heat Exchanger surge tank exhaust steam condensation-water drain of described First Heat Exchanger is connected with the surge tank exhaust steam condensed water water inlet pipe of condensation water collection tank, the condensation water collection tank outlet pipe of described condensation water collection tank is connected with the entrance of the second water pump, and the outlet of described the second water pump accesses in described pressure-bearing surge tank, the First Heat Exchanger circulating cooling water inlet of described First Heat Exchanger and First Heat Exchanger circulating cooling water out connect and compose circulation with outside circulating cooling water pipe respectively, the 3rd control valve is installed on the inlet duct of First Heat Exchanger circulating cooling water inlet, the first incoagulable gas delivery pipe stretching out is straight up installed on the outlet of First Heat Exchanger surge tank exhaust steam condensation-water drain, in described pressure-bearing surge tank, be provided with the surge tank outlet pipe of opening upwards, 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 the first water delivery side of pump is through a deoxygenation 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 the 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 a deoxygenation gland steam exhauster of discharge deoxygenation exhaust steam and incoagulable gas, the outlet of a described deoxygenation gland steam exhauster is connected with the second heat exchanger deoxygenation exhaust steam import of the second heat exchanger, and the second heat exchanger deoxygenation exhaust steam condensation-water drain of described the second heat exchanger is connected with the deoxygenation exhaust steam condensed water water inlet pipe of condensation water collection tank, the second heat exchanger circulating cooling water inlet of described the second heat exchanger and the second heat exchanger circulating cooling water out connect and compose circulation with outside circulating cooling water pipe respectively, the 6th control valve is installed on the inlet duct of the second heat exchanger circulating cooling water inlet, the second incoagulable gas delivery pipe stretching out is straight up installed on the outlet of the second heat exchanger deoxygenation exhaust steam condensation-water drain, 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, and the second control valve is installed on described blow-off pipe.
With respect to prior art, the present invention has obtained following beneficial effect: (1) calcining furnace condensed water, fluid bed condensed water, synthetic ammonia cooling and desalting water and conversion cooling and desalting water enter respectively in pressure-bearing surge tank, after mixing, discharge from surge tank outlet pipe, 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; The incoagulable gas such as the oxygen overflowing in a deoxygenation deoxygenation exhaust steam that steam mixing produces and water are discharged from a deoxygenation gland steam exhauster of deoxygenation crown portion.Pressure-bearing surge tank can bearing certain pressure and water level can in a big way, adjust, can make up the contradiction between the intermittence of boiler replenishing water and the continuity of condensed water generation, between by vapour unit and boiler replenishing water system, form isolation and buffering, the fluctuation of guaranteeing 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 and fluidized system occur that the row's of building the pressure condensed water is not smooth; Also avoided in the time of 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 contain the incoagulable gas such as oxygen, the incoagulable gas such as the high and oxygen-free gas of calcining furnace condensed water and fluid bed condensate temperature, temperature rise after cooling and desalting water mixes with steam condensate (SC), and pressure-bearing surge tank operating pressure is saturation pressure 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, after overflowing the pressure-bearing surge tank water surface, discharge from surge tank gland steam exhauster with surge tank exhaust steam, realize one-level deoxygenation; Sent into a deoxygenation water inlet pipe of higher-pressure deaerator through the first water pump and the 5th control valve by the discharge of surge tank outlet pipe through the water of one-level deoxygenation, external steam enters deoxygenation head to carrying out secondary deoxygenation from deoxygenation steam pipe and the 4th control valve, a deoxygenation steam mixes the incoagulable gas such as deoxygenation exhaust steam and oxygen producing discharges from a deoxygenation gland steam exhauster, sends into boiler as boiler replenishing water through the water of secondary deoxygenation by the 3rd water pump.(4) the non-return valve on surge tank gland steam exhauster can guarantee that atmosphere can not pour in down a chimney to pressure-bearing surge tank, prevents from introducing extraneous oxygen.(5) the first control valve, by controlling the discharge capacity of surge tank exhaust steam, makes to maintain certain pressure in pressure-bearing surge tank, to fully 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, reduced unit steam coal consumption.(7) synthetic ammonia cooling and desalting water, conversion cooling and desalting water first water inlet pipe and three water inlet pipe higher from position that temperature is relatively low, density is higher enter, calcining furnace condensed water, fluid bed condensed water second water inlet pipe and four water inlet pipe lower from position that temperature is relatively high, density is lower enters pressure-bearing surge tank, can in pressure-bearing surge tank, form free convection, promote abundant heat exchange.(8) along with the increase of working time, certain impurity can be gathered in pressure-bearing surge tank bottom, and water quality can decline, and now can open the second control valve, discharges the water of water quality variation from blow-off pipe, guarantees boiler replenishing water water quality.(9) the surge tank exhaust steam of pressure-bearing surge tank discharge enters First Heat Exchanger and is recycled cooling water and is condensed into surge tank exhaust steam condensed water after indirectly cooling and enters in condensation water collection tank, fill into pressure-bearing surge tank by the second water pump, reclaimed entrained most of water and the part heat of surge tank exhaust steam.(10) after surge tank exhaust steam condensation, the incoagulable gas such as the oxygen of discharging with surge tank exhaust steam are still gaseous state, discharge from the first incoagulable gas delivery pipe; Incoagulable gas density is little, and the first incoagulable gas delivery pipe stretches out the discharge that is beneficial to incoagulable gas straight up.(11) the deoxygenation exhaust steam of higher-pressure deaerator discharge enters the second heat exchanger and is recycled cooling water and is condensed into deoxygenation exhaust steam condensed water after indirectly cooling and enters in condensation water collection tank, fill into pressure-bearing surge tank by the second water pump, reclaimed entrained most of water and the part heat of deoxygenation exhaust steam.(12) after deoxygenation exhaust steam condensation, the incoagulable gas such as the oxygen of discharging with deoxygenation exhaust steam are still gaseous state, discharge from the second incoagulable gas delivery pipe; Incoagulable gas density is little, and the second incoagulable gas delivery pipe stretches out the discharge that is beneficial to incoagulable gas straight up.
As preferred version of the present invention, the mouth of pipe that described the 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 with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, the middle and lower part of each described annular water distributor is evenly distributed with respectively to the spray-hole of the axis jet of pressure-bearing surge tank, the axis of each described spray-hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by having arranged ring pipe water outlet in the tank of spray-hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extended with tank in time of contact of water body, realize abundant heat exchange, avoid thermal explosion.
As preferred version of the present invention, the inner chamber middle and lower part of described pressure-bearing surge tank is provided with Forced Mixing impeller, described Forced Mixing impeller is fixedly connected on Forced Mixing impeller shaft, described Forced Mixing impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.In the time that the temperature difference of calcining furnace condensed water, fluid bed condensed water and synthetic ammonia cooling and desalting water, conversion cooling and desalting water is larger, only depend on natural heat-exchange, in tank, temperature is still difficult to be evenly distributed, easily in pressure-bearing surge tank, formation temperature is poor, now open Forced Mixing impeller tank inner storing water is carried out to Forced Mixing, promote the uniformity of Temperature Distribution in tank.
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 shaft, described disturbance impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of described disturbance impeller shaft is connected with disturbance impeller drive motor; Described disturbance impeller shaft 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 extends perpendicular to base plate and along base plate diametric(al).In the time of needs blowdown, impurity often accumulates in the bottom of pressure-bearing surge tank, is difficult to discharge with current, now opens disturbance impeller bottom water flow rotation can be flashed impurity; If current are stable circulation state, good not to the disturbance effect of impurity, disturbance impeller shaft of the present invention departs from the axis of pressure-bearing surge tank, can avoid making current to present stable circulation state; The eddy current baffle plate that plate inner wall is installed can thoroughly 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 two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different-diameter of base plate.The more sewage draining exit that distributes in multiple orientation of base plate, can improve contaminant removal effectiveness, reduces 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 are staggered in a circumferential direction, centered by pressure-bearing surge tank axis, be equipped with sewage draining exit to extraradial eight directions, can making blowdown 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, described sampling pipe stretches out outside pressure-bearing surge tank and with sampling cooler and is connected, and online electric conductivity detector and online Ph value detector are installed on the export pipeline of described sampling cooler.Can detect in real time in-tank mixing electrical conductivity of water and Ph value.
As preferred version of the present invention, the holding wire of described online electric conductivity detector and online Ph value detector accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of described PLC controller is connected with the control line of described the second control valve; In the time that PLC controller detects that Ph value that electrical conductivity that online electric conductivity detector provides is greater than setting value or online Ph value detector and provides exceedes setting range, control the second control valve and open, set value and Ph value detector provides online Ph value is controlled the second control valve in setting range time and closed when PLC controller detects that electrical conductivity that online electric conductivity detector provides is less than.The Ph value that the electrical conductivity that PLC controller can provide according to online electric conductivity detector and online Ph value detector provide, the keying of control disturbance impeller and the second control valve automatically, the automatization level of raising system.
As preferred version of the present invention, on described the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, be separately installed with temperature sensor and flowmeter, the different azimuth of the liquid Space of described pressure-bearing surge tank and differing heights are provided with multiple temperature sensors altogether; The gas-phase space of described pressure-bearing surge tank is provided with pressure sensor; The holding wire of described pressure sensor, each described temperature sensor and each described flowmeter accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of described PLC controller is connected with the control line of described the first control valve; The aperture of controlling the first control valve in the time that PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve in the time that PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of described pressure-bearing surge tank liquid Space, the force value that p surveys for described pressure sensor; T0 is the set temperature value of PLC controller, 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 first, second, third and the 4th temperature sensor on water inlet pipe detects, and m1, m2, m3 and m4 are respectively first, second, third and the 4th measured flow of flowmeter on water inlet pipe; P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.Temperature sensor can detect the water temperature of each water inlet pipe and pressure-bearing surge tank, and flowmeter can be measured the actual flow of each water inlet pipe; The set temperature value of PLC controller is got the weighted average water temperature t0 of each water inlet pipe, there is one-to-one relationship in saturation pressure p0 and the water temperature t0 of water vapour, in the time that temperature in tank is greater than design temperature or tank internal pressure and is greater than setting pressure, the aperture of PLC controller control the first control valve strengthens, to strengthen the discharge of surge tank exhaust steam; When temperature in tank is lower than design temperature or tank internal pressure during lower than setting pressure, the aperture of PLC controller control the first control valve reduces, and prevents from that steam discharge is excessive even to occur that tank outer air pours in down a chimney; Adopt PLC controller automatically to regulate the aperture of the first control valve according to water temperature and pressure, improved the automatization level of system, avoid the excess discharge of surge tank exhaust steam, guarantee that pressure-bearing surge tank is operated at the maximum pressure/temperature of permission, not only energy-conservation but also environmental protection.
As preferred version of the present invention, the 9th temperature sensor of surveying surge tank exhaust steam condensate temperature is installed on the outlet of described First Heat Exchanger surge tank exhaust steam condensation-water drain, the corresponding signal input of the holding wire access PLC controller of described the 9th temperature sensor, the corresponding signal output of described PLC controller is connected with the control line of described the 3rd control valve, and the temperature height that described PLC controller detects according to the 9th temperature sensor is controlled the aperture size of the 3rd control valve; The tenth temperature sensor of surveying deoxygenation exhaust steam condensate temperature is installed on the outlet of described the second heat exchanger deoxygenation exhaust steam condensation-water drain, the corresponding signal input of the holding wire access PLC controller of described the tenth temperature sensor, the corresponding signal output of described PLC controller is connected with the control line of described the 6th control valve, and the temperature height that described PLC controller detects according to the tenth temperature sensor is controlled the aperture size of the 6th control valve.
Brief description of the drawings
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, non-in order to limit the present invention.
Fig. 1 is that condensed water demineralized water of the present invention mixes the schematic diagram that reclaims surge tank and deoxygenation exhaust steam condensing unit.
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;
PLC.PLC controller;
E1. pressure-bearing surge tank; E1a. sewage draining exit; E1b. eddy current baffle plate; E1c. Forced Mixing impeller; 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 flow meter; M2. the second flowmeter; M3. the 3rd flowmeter; M4. the 4th flowmeter;
Q. the cooler of sampling; Q1. online electric conductivity detector; Q2. online Ph value detector;
H1. First Heat Exchanger; H1a. First Heat Exchanger circulating cooling water inlet; H1b. First Heat Exchanger circulating cooling water out; H1c. First Heat Exchanger surge tank exhaust steam import; H1d. First Heat Exchanger surge tank exhaust steam condensation-water drain; H1e. the first incoagulable gas delivery pipe; T9. the 9th temperature sensor; V3. the 3rd control valve;
E2. condensation water collection tank; E2a. condensation water collection tank outlet pipe; E2b. surge tank exhaust steam condensed water water inlet pipe; E2c. deoxygenation exhaust steam condensed water water inlet pipe; B2. the second water pump;
E3. higher-pressure deaerator; E3a. deoxygenation steam pipe; E3b. a deoxygenation water inlet pipe; E3c. a deoxygenation gland steam exhauster; E3d. deoxygenation case drainpipe; B3. the 3rd water pump; V4. the 4th control valve; V5. the 5th control valve;
H2. the second heat exchanger; H2a. the second heat exchanger circulating cooling water inlet; H2b. the second heat exchanger circulating cooling water out; H2c. the second heat exchanger deoxygenation exhaust steam import; H2d. the second heat exchanger deoxygenation exhaust steam condensation-water drain; H2e. the second incoagulable gas delivery pipe; T10. the tenth temperature sensor; V6. the 6th control valve.
Detailed description of the invention
As shown in Figure 1, condensed water demineralized water of the present invention mixes recovery surge tank and deoxygenation exhaust steam condensing unit, comprise the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, the fluid bed condensed water of 135 DEG C ~ 155 DEG C, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C, also comprise the pressure-bearing surge tank E1 of sealing.On the circumference of pressure-bearing surge tank E1, be 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, in the relative and short transverse of the mouth of pipe of the first water inlet pipe G1 and the 3rd water inlet pipe G3, mutually stagger, in the relative and short transverse of the mouth of pipe of the second water inlet pipe G2 and the 4th water inlet pipe G4, mutually stagger, 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.Synthetic ammonia cooling and desalting water and conversion cooling and desalting water access respectively the first water inlet pipe G1 and the 3rd water inlet pipe G3, and calcining furnace condensed water and fluid bed condensed water access respectively the second water inlet pipe G2 and the 4th water inlet pipe G4; The roof middle part of pressure-bearing surge tank E1 is connected with surge tank gland steam exhauster G5, and non-return valve Vd and the first control valve V1 are installed on surge tank gland steam exhauster G5 from lower to upper successively.
The outlet of the first control valve V1 is connected with the First Heat Exchanger surge tank exhaust steam import H1c of First Heat Exchanger H1, the First Heat Exchanger surge tank exhaust steam condensation-water drain H1d of First Heat Exchanger H1 is connected with the surge tank exhaust steam condensed water water inlet pipe E2b of condensation water collection tank E2, the condensation water collection tank outlet pipe E2a of condensation water collection tank E2 is connected with the entrance of the second water pump B2, in the outlet access pressure-bearing surge tank E1 of the second water pump B2, the First Heat Exchanger circulating cooling water inlet H1a of First Heat Exchanger H1 and First Heat Exchanger circulating cooling water out H1b connect and compose circulation with outside circulating cooling water pipe respectively, be that First Heat Exchanger circulating cooling water inlet H1a is connected with the circulating cooling water pipe of low temperature, First Heat Exchanger circulating cooling water out H1b is connected with the circulating cooling water pipe of high temperature, on the inlet duct of First Heat Exchanger circulating cooling water inlet H1a, the 3rd control valve V3 is installed, the the first incoagulable gas delivery pipe H1e stretching out is straight up installed on the outlet of First Heat Exchanger surge tank exhaust steam condensation-water drain H1d, on the first incoagulable gas delivery pipe H1e, stop valve is installed.The first incoagulable gas delivery pipe H1e is preferably installed on the highest point of First Heat Exchanger surge tank exhaust steam condensating water outlet tube, and the best is installed on the descending opposite direction of turning round of First Heat Exchanger surge tank exhaust steam condensating water outlet tube.
In pressure-bearing surge tank E1, be provided with the surge tank outlet pipe G6 of opening upwards, 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 is through a deoxygenation water inlet pipe E3b of the 5th control valve V5 access higher-pressure deaerator E3, the entrance of deoxygenation case drainpipe E3d access the 3rd water pump B3 of higher-pressure deaerator E3, the outlet access boiler replenishing water pipe of the 3rd water pump B3, external steam is by the 4th control valve V4 access deoxygenation steam pipe E3a, the deoxygenation crown portion of higher-pressure deaerator E3 is connected with a deoxygenation gland steam exhauster E3c of discharge deoxygenation exhaust steam and incoagulable gas.
A deoxygenation gland steam exhauster E3c is connected with the second heat exchanger deoxygenation exhaust steam import H2c of the second heat exchanger H2, and the second heat exchanger deoxygenation exhaust steam condensation-water drain H2d of the second heat exchanger H2 is connected with the deoxygenation exhaust steam condensed water water inlet pipe E2c of condensation water collection tank E2, the second heat exchanger circulating cooling water inlet H2a of the second heat exchanger H2 and the second heat exchanger circulating cooling water out H2b connect and compose circulation with outside circulating cooling water pipe respectively, the second heat exchanger circulating cooling water inlet H2a is connected with the circulating cooling water pipe of low temperature, the second heat exchanger circulating cooling water out H2b is connected with the circulating cooling water pipe of high temperature, on the inlet duct of the second heat exchanger circulating cooling water inlet H2a, the 6th control valve V6 is installed, the the second incoagulable gas delivery pipe H2e stretching out is straight up installed on the outlet of the second heat exchanger deoxygenation exhaust steam condensation-water drain H2d, on the second incoagulable gas delivery pipe H2e, stop valve is installed.The second incoagulable gas delivery pipe H2e is preferably installed on the highest point of the second heat exchanger deoxygenation exhaust steam condensating water outlet tube, and the best is installed on the descending opposite direction of turning round of the second heat exchanger deoxygenation exhaust steam condensating water outlet tube.
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, and the second control valve V2 is installed on blow-off pipe G7.
When work, from position, higher the first water inlet pipe G1 and the 3rd water inlet pipe G3 enters respectively for the synthetic ammonia cooling and desalting water that temperature is relatively low, density is higher and conversion cooling and desalting water; The second water inlet pipe G2 and the 4th water inlet pipe G4 that the calcining furnace condensed water that temperature is relatively high, density is lower and fluid bed condensed water are lower from position enter pressure-bearing surge tank E1, can in pressure-bearing surge tank, form free convection, promote abundant heat exchange.Synthetic ammonia cooling and desalting water, conversion cooling and desalting water are discharged from surge tank outlet pipe G6 after mixing with calcining furnace condensed water, fluid bed condensed water, send into higher-pressure deaerator E3 carry out secondary deoxygenation by the first water pump B1.The temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and contain the incoagulable gas such as oxygen, the incoagulable gas such as the high and oxygen-free gas of calcining furnace condensed water and fluid bed condensate temperature, synthetic ammonia cooling and desalting water, conversion cooling and desalting water and calcining furnace condensed water, temperature rise after fluid bed condensed water mixes, and pressure-bearing surge tank E1 operating pressure is saturation pressure 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, after overflowing the pressure-bearing surge tank water surface, discharge from surge tank gland steam exhauster G5 with surge tank exhaust steam, realize one-level deoxygenation, sent into a deoxygenation water inlet pipe E3b of higher-pressure deaerator E3 through the first water pump B1 and the 5th control valve V5 by surge tank outlet pipe G6 discharge through the water of one-level deoxygenation, external steam enters deoxygenation head to carrying out secondary deoxygenation from deoxygenation steam pipe E3a and the 4th control valve V4, the incoagulable gas such as deoxygenation exhaust steam and oxygen are discharged from a deoxygenation 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.
The deoxygenation exhaust steam of discharging from a deoxygenation gland steam exhauster E3c enters the second heat exchanger H2 by the second heat exchanger deoxygenation exhaust steam import H2c, being recycled cooling water becomes deoxygenation exhaust steam condensed water after indirectly cooling and discharges from the second heat exchanger deoxygenation exhaust steam condensation-water drain H2d, this deoxygenation exhaust steam condensed water enters condensation water collection tank E2 from deoxygenation exhaust steam condensed water water inlet pipe E2c, enter the second water pump B2 from condensation water collection tank outlet pipe E2a again, the second water pump B2 is pumped in pressure-bearing surge tank E1, the incoagulable gas such as the oxygen of discharging with deoxygenation exhaust steam are discharged from the second incoagulable gas delivery pipe H2e.
Surge tank exhaust steam enters First Heat Exchanger H1 from First Heat Exchanger surge tank exhaust steam import H1c, being recycled cooling water becomes surge tank exhaust steam condensed water after indirectly cooling and discharges from First Heat Exchanger surge tank exhaust steam condensation-water drain H1d, this surge tank exhaust steam condensed water enters condensation water collection tank E2 from surge tank exhaust steam condensed water water inlet pipe E2b, enter the second water pump B2 from condensation water collection tank outlet pipe E2a again, the incoagulable gas such as the second water pump B2 is pumped in pressure-bearing surge tank E1, the oxygen of discharging with surge tank exhaust steam are discharged from the first incoagulable gas delivery pipe H1e.Non-return valve Vd on surge tank gland steam exhauster G5 can guarantee that atmosphere can not pour in down a chimney to pressure-bearing surge tank E1, prevents from introducing extraneous oxygen.The 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, to fully 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, reduced unit steam coal consumption.Along with the increase of working time, pressure-bearing surge tank E1 can gather certain impurity in bottom, and water quality can decline, and now can open the second control valve V2, and the water of discharging water quality variation from blow-off pipe G7, guarantees boiler replenishing water water quality.
As improvement, the first temperature sensor T1 and first flow meter M1 are installed on the first water inlet pipe G1, the second temperature sensor T2 and the second flowmeter M2 are installed on the second water inlet pipe G2, three-temperature sensor T3 and the 3rd flowmeter M3 are installed on the 3rd water inlet pipe G3, the 4th temperature sensor T4 and the 4th flowmeter M4 are installed on the 4th water inlet pipe G4.Different azimuth and the differing heights of the liquid Space of pressure-bearing surge tank E1 are provided with multiple temperature sensors altogether, for example 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 flow meter M1, the second flowmeter M2, the 3rd flowmeter M3, the 4th flowmeter M4 and pressure sensor P accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of PLC controller is connected with the control line of the first control valve V1.
The aperture of controlling the first control valve V1 in the time that PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve V1 in the time that PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of pressure-bearing surge tank liquid Space, for example, be the mean value of the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor water temperature that T8 surveys; The force value that p surveys for pressure sensor P; T0 is the set temperature value of PLC controller, 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 flow meter M1, the second flowmeter M2, the 3rd flowmeter M3 and the measured flow of the 4th flowmeter M4.P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
The set temperature value of PLC controller is got the weighted average water temperature t0 of each water inlet pipe, there is one-to-one relationship in saturation pressure p0 and the water temperature t0 of water vapour, in the time that temperature in tank is greater than design temperature or tank internal pressure and is greater than setting pressure, the aperture of PLC controller control the first control valve V1 strengthens, to strengthen the discharge of surge tank exhaust steam; When temperature in tank is lower than design temperature or tank internal pressure during lower than setting pressure, the aperture of PLC controller control the first control valve V1 reduces, and prevents from that steam discharge is excessive even to occur that tank outer air pours in down a chimney.Adopt PLC controller automatically to regulate the aperture of the first control valve V1 according to water temperature and pressure, improved the automatization level of system, avoid the excess discharge of surge tank exhaust steam, guarantee that pressure-bearing surge tank is operated at the maximum pressure/temperature of permission, not only energy-conservation but also environmental protection.
As improvement, the 9th temperature sensor T9 that surveys surge tank exhaust steam condensate temperature is installed on the outlet of First Heat Exchanger surge tank exhaust steam condensation-water drain H1d, the 9th temperature sensor T9 can detect the temperature of the surge tank exhaust steam condensed water of arranging of First Heat Exchanger H1, the corresponding signal input of the holding wire access PLC controller of the 9th temperature sensor, the corresponding signal output of PLC controller is connected with the control line of the 3rd control valve V3, the temperature height that PLC controller detects according to the 9th temperature sensor T9 is controlled the aperture size of the 3rd control valve V3, to control the cooling water flow that enters First Heat Exchanger H1.
As improvement, the tenth temperature sensor T10 that surveys deoxygenation exhaust steam condensate temperature is installed on the outlet of the second heat exchanger deoxygenation exhaust steam condensation-water drain H2d, the tenth temperature sensor T10 can detect the second heat exchanger H2 get rid of the temperature of oxygen exhaust steam condensed water, the corresponding signal input of the holding wire access PLC controller of the tenth temperature sensor, the corresponding signal output of PLC controller is connected with the control line of the 6th control valve V6, the temperature height that PLC controller detects according to the tenth temperature sensor T10 is controlled the aperture size of the 6th control valve V6, to control the cooling water flow that enters the second heat exchanger H2.
The intracavity bottom of pressure-bearing surge tank E1 can be provided with sampling pipe E1e, sampling pipe E1e stretches out outside pressure-bearing surge tank E1 and with sampling cooler Q and is connected, online electric conductivity detector Q1 and online Ph value detector Q2 are installed, to detect in real time in-tank mixing electrical conductivity of water and Ph value on the export pipeline of sampling cooler Q.
For improving the automatization level of system, the holding wire of online electric conductivity detector Q1 and online Ph value detector Q2 accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of PLC controller is connected with the control line of the second control valve V2; In the time that PLC controller detects that 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 exceedes setting range, controlling the second control valve V2 opens, when PLC controller detects that electrical conductivity that online electric conductivity detector Q1 provides is less than Ph value that setting value and online Ph value detector Q2 provide and controls the second control valve V2 in setting range time and close, the electrical conductivity providing according to online electric conductivity detector Q1 and the Ph value that Ph value detector Q2 provides are online provided, automatically control the keying of the second control valve V2.
As shown in Figure 2, as improvement, the mouth of pipe that 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 are positioned at pressure-bearing surge tank is connected with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, in Fig. 2 taking the 3rd water inlet pipe G3 as example, the middle and lower part of each annular water distributor is evenly distributed with respectively to the spray-hole of the axis jet of pressure-bearing surge tank, the axis of each spray-hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by having arranged ring pipe water outlet in the tank of spray-hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extended with tank in time of contact of water body, realize abundant heat exchange, avoid thermal explosion.
As shown in Figure 1, in the time that the temperature difference of calcining furnace condensed water, fluid bed condensed water and synthetic ammonia cooling and desalting water, conversion cooling and desalting water is larger, only depend on natural heat-exchange, in tank, temperature is still difficult to be evenly distributed, and easily in pressure-bearing surge tank E1, formation temperature is poor.Forced Mixing impeller E1c can be installed in the inner chamber middle and lower part of pressure-bearing surge tank, Forced Mixing impeller E1c is fixedly connected on Forced Mixing impeller shaft, Forced Mixing impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor, and Forced Mixing impeller shaft is preferably placed on the axis of pressure-bearing surge tank.Open Forced Mixing impeller E1c tank inner storing water is carried out to Forced Mixing, promote the uniformity of Temperature Distribution in tank.
Because impurity accumulates in the bottom of pressure-bearing surge tank, when blowdown, be difficult to discharge with current, can disturbance impeller E1d be installed at the intracavity bottom of pressure-bearing surge tank, disturbance impeller E1d is fixedly connected on disturbance impeller shaft, disturbance impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of disturbance impeller shaft is connected with disturbance impeller drive motor, opens disturbance impeller E1d bottom water flow rotation can be flashed impurity, is beneficial to discharge.
Disturbance impeller shaft 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 extends perpendicular to base plate and along base plate diametric(al), eddy current baffle plate E1b can thoroughly 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, for example be divided into two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, 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 are staggered in a circumferential direction, the 45 ° of settings of staggering successively in phase place, four inner ring sewage draining exits layout that assumes diamond in shape, 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 present invention's better possible embodiments, 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, and whole device can share a PLC controller, also can each unit by PLC controller control separately.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop in the protection domain of requirement of the present invention.
Claims (10)
1. a condensed water demineralized water mixes recovery surge tank and deoxygenation exhaust steam condensing unit, comprise the calcining furnace condensed water of 135 DEG C ~ 155 DEG C, the fluid bed condensed water of 135 DEG C ~ 155 DEG C, the conversion cooling and desalting water of the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and 60 DEG C ~ 95 DEG C, it is characterized in that: the pressure-bearing surge tank that also comprises sealing, on the circumference of described pressure-bearing surge tank, be vertically connected with the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, in the relative and short transverse of the mouth of pipe of described the first water inlet pipe and the 3rd water inlet pipe, mutually stagger, in the relative and short transverse of the mouth of pipe of described the second water inlet pipe and the 4th water inlet pipe, mutually stagger, the height of described the first water inlet pipe and the 3rd water inlet pipe is higher than described the second water inlet pipe and the 4th water inlet pipe, described synthetic ammonia cooling and desalting water and conversion cooling and desalting water access respectively described the first water inlet pipe and the 3rd water inlet pipe, and described calcining furnace condensed water and fluid bed condensed water access respectively described the second water inlet pipe and the 4th water inlet pipe, the roof middle part of described pressure-bearing surge tank is connected with surge tank gland steam exhauster, and non-return valve and the first control valve are installed on described surge tank gland steam exhauster from lower to upper successively, the outlet of described the first control valve is connected with the First Heat Exchanger surge tank exhaust steam import of First Heat Exchanger, the First Heat Exchanger surge tank exhaust steam condensation-water drain of described First Heat Exchanger is connected with the surge tank exhaust steam condensed water water inlet pipe of condensation water collection tank, the condensation water collection tank outlet pipe of described condensation water collection tank is connected with the entrance of the second water pump, and the outlet of described the second water pump accesses in described pressure-bearing surge tank, the First Heat Exchanger circulating cooling water inlet of described First Heat Exchanger and First Heat Exchanger circulating cooling water out connect and compose circulation with outside circulating cooling water pipe respectively, the 3rd control valve is installed on the inlet duct of First Heat Exchanger circulating cooling water inlet, the first incoagulable gas delivery pipe stretching out is straight up installed on the outlet of First Heat Exchanger surge tank exhaust steam condensation-water drain, in described pressure-bearing surge tank, be provided with the surge tank outlet pipe of opening upwards, 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 the first water delivery side of pump is through a deoxygenation 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 the 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 a deoxygenation gland steam exhauster of discharge deoxygenation exhaust steam and incoagulable gas, the outlet of a described deoxygenation gland steam exhauster is connected with the second heat exchanger deoxygenation exhaust steam import of the second heat exchanger, and the second heat exchanger deoxygenation exhaust steam condensation-water drain of described the second heat exchanger is connected with the deoxygenation exhaust steam condensed water water inlet pipe of condensation water collection tank, the second heat exchanger circulating cooling water inlet of described the second heat exchanger and the second heat exchanger circulating cooling water out connect and compose circulation with outside circulating cooling water pipe respectively, the 6th control valve is installed on the inlet duct of the second heat exchanger circulating cooling water inlet, the second incoagulable gas delivery pipe stretching out is straight up installed on the outlet of the second heat exchanger deoxygenation exhaust steam condensation-water drain, 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, and the second control valve is installed on described blow-off pipe.
2. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: described the first water inlet pipe, the second water inlet pipe, the mouth of pipe that the 3rd water inlet pipe and the 4th water inlet pipe are positioned at pressure-bearing surge tank is connected with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, the middle and lower part of each described annular water distributor is evenly distributed with respectively to the spray-hole of the axis jet of pressure-bearing surge tank, the axis of each described spray-hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.
3. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: the inner chamber middle and lower part of described pressure-bearing surge tank is provided with Forced Mixing impeller, described Forced Mixing impeller is fixedly connected on Forced Mixing impeller shaft, described Forced Mixing impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.
4. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, 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 shaft, described disturbance impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate realize sealing, the lower end of described disturbance impeller shaft is connected with disturbance impeller drive motor; Described disturbance impeller shaft 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 extends perpendicular to base plate and along base plate diametric(al).
5. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: described sewage draining exit is provided with multiple, be divided into two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different-diameter of base plate.
6. condensed water demineralized water according to claim 5 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, 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 °.
7. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with sampling pipe, described sampling pipe stretches out outside pressure-bearing surge tank and with sampling cooler and is connected, and online electric conductivity detector and online Ph value detector are installed on the export pipeline of described sampling cooler.
8. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: the holding wire of described online electric conductivity detector and online Ph value detector accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of described PLC controller is connected with the control line of described the second control valve; In the time that PLC controller detects that Ph value that electrical conductivity that online electric conductivity detector provides is greater than setting value or online Ph value detector and provides exceedes setting range, control the second control valve and open, set value and Ph value detector provides online Ph value is controlled the second control valve in setting range time and closed when PLC controller detects that electrical conductivity that online electric conductivity detector provides is less than.
9. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: on described the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, be separately installed with temperature sensor and flowmeter, the different azimuth of the liquid Space of described pressure-bearing surge tank and differing heights are provided with multiple temperature sensors altogether; The gas-phase space of described pressure-bearing surge tank is provided with pressure sensor; The holding wire of described pressure sensor, each described temperature sensor and each described flowmeter accesses respectively the corresponding signal input of PLC controller, and the corresponding signal output of described PLC controller is connected with the control line of described the first control valve; The aperture of controlling the first control valve in the time that PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve in the time that PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of described pressure-bearing surge tank liquid Space, the force value that p surveys for described pressure sensor; T0 is the set temperature value of PLC controller, 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 first, second, third and the 4th temperature sensor on water inlet pipe detects, and m1, m2, m3 and m4 are respectively first, second, third and the 4th measured flow of flowmeter on water inlet pipe; P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapour corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
10. condensed water demineralized water according to claim 1 mixes recovery surge tank and deoxygenation exhaust steam condensing unit, it is characterized in that: the 9th temperature sensor of surveying surge tank exhaust steam condensate temperature is installed on the outlet of described First Heat Exchanger surge tank exhaust steam condensation-water drain, the corresponding signal input of the holding wire access PLC controller of described the 9th temperature sensor, the corresponding signal output of described PLC controller is connected with the control line of described the 3rd control valve, the temperature height that described PLC controller detects according to the 9th temperature sensor is controlled the aperture size of the 3rd control valve, the tenth temperature sensor of surveying deoxygenation exhaust steam condensate temperature is installed on the outlet of described the second heat exchanger deoxygenation exhaust steam condensation-water drain, the corresponding signal input of the holding wire access PLC controller of described the tenth temperature sensor, the corresponding signal output of described PLC controller is connected with the control line of described the 6th control valve, and the temperature height that described PLC controller detects according to the tenth temperature sensor is controlled the aperture size of the 6th control valve.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108194822A (en) * | 2018-01-31 | 2018-06-22 | 维度绿色科技（广州）有限公司 | A kind of continuous hydrophobic device with flash-off steam pressure recovery |
| CN108443861A (en) * | 2018-05-25 | 2018-08-24 | 安徽中烟工业有限责任公司 | A kind of energy saver for eliminating enclosed condensation water recovery system back pressure |
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| 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 |
| CN103499089A (en) * | 2013-09-25 | 2014-01-08 | 济南澳海炭素有限公司 | Exhaust steam recycling heating device for waste heat power generation deaerator |
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| 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 |
| CN103499089A (en) * | 2013-09-25 | 2014-01-08 | 济南澳海炭素有限公司 | Exhaust steam recycling heating device for waste heat power generation deaerator |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108194822A (en) * | 2018-01-31 | 2018-06-22 | 维度绿色科技（广州）有限公司 | A kind of continuous hydrophobic device with flash-off steam pressure recovery |
| CN108443861A (en) * | 2018-05-25 | 2018-08-24 | 安徽中烟工业有限责任公司 | A kind of energy saver for eliminating enclosed condensation water recovery system back pressure |
| CN108443861B (en) * | 2018-05-25 | 2023-11-03 | 安徽中烟工业有限责任公司 | Energy-saving device for eliminating back pressure of closed condensate water recovery system |
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