CN103787434A - Power-water-salt coproduction process for condensing steam turbine generator unit - Google Patents
Power-water-salt coproduction process for condensing steam turbine generator unit Download PDFInfo
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- CN103787434A CN103787434A CN201310729374.2A CN201310729374A CN103787434A CN 103787434 A CN103787434 A CN 103787434A CN 201310729374 A CN201310729374 A CN 201310729374A CN 103787434 A CN103787434 A CN 103787434A
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- turbine generator
- steam turbine
- salt
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- 238000000034 method Methods 0.000 title claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 150000003839 salts Chemical class 0.000 claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 16
- 239000013505 freshwater Substances 0.000 claims abstract description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims description 51
- 239000013535 sea water Substances 0.000 claims description 51
- 239000012267 brine Substances 0.000 claims description 19
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 19
- 239000012266 salt solution Substances 0.000 claims description 16
- 230000005611 electricity Effects 0.000 claims description 14
- 230000004087 circulation Effects 0.000 claims description 11
- 238000009835 boiling Methods 0.000 claims description 9
- 238000007670 refining Methods 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 8
- 239000003513 alkali Substances 0.000 claims description 7
- 235000017550 sodium carbonate Nutrition 0.000 claims description 7
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 230000001839 systemic circulation Effects 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- 241001131796 Botaurus stellaris Species 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 6
- 239000002826 coolant Substances 0.000 abstract description 4
- 238000010248 power generation Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 6
- 239000013589 supplement Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 235000019600 saltiness Nutrition 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000007738 vacuum evaporation Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a power-water-salt coproduction process for a condensing steam turbine generator unit, and in particular relates to production of liquid salt water serving as a raw material for use in production of a chloro-alkaline or sodium carbonate system and coproduction of fresh water by using negative-pressure steam exhausted by the condensing steam turbine generator unit after power generation. The power-water-salt coproduction process for the condensing steam turbine generator unit comprises the following steps: driving the condensing steam turbine generator unit to run by using steam generated in a previous-stage process in order to generate power; introducing tail steam being lower than -0.04MPa in surface pressure exhausted from the condensing steam turbine generator unit into a heat exchanger to undergo heat exchange with a cooling medium extracted from a storage tank through a forced circulating pump in order to condense the tail steam into water; and performing steam-liquid separation in a steam trap, and returning into a boiler water treatment system for recycling. The power-water-salt coproduction process for the condensing steam turbine generator unit is simple in process, and can be used for realizing power-water-salt coproduction.
Description
Technical field
The present invention relates to condensing steam turbine generator group electricity, water, salt joint process, be specially negative pressure steam that condensing steam turbine generator group discharges after generating be used for production liquid brine as raw material for chlor-alkali or the production of soda ash system, and coproduction fresh water.
Background technology
Thermal power generation at present is substantially divided into counter pressure turbine generating, condensing steam turbine generating, takes out three kinds of forms of condensing steam turbine generating, counter pressure turbine generating feature is that steam turbine end steam outlet pressure is greater than normal pressure, the steam of discharging is commonly used for other technique (such as warming), its generating efficiency is lower than condensing steam turbine generating and take out the generating of condensing-type steamer, but the latent heat enthalpy of steam is utilized substantially; Condensing steam turbine generating feature is: steam turbine end outlet pressure is lower than normal pressure, it is negative pressure state, generating efficiency is the highest, but the latent heat enthalpy of steam is not utilized, the heat utilization rate less than 45% of whole system, takes out condensing steam turbine generator between above-mentioned two kinds of techniques, is characterized in extracting the hot user of steam supply with certain pressure out from steam turbine intermediate stage, remaining steam continues the blade acting at drive rotor rear portion, then reclaims water of condensation.Because the steam latent heat enthalpy of extracting part out has obtained utilization, and the steam enthalpy of condensation portion is not utilized, and therefore its utilization efficiency of heat energy is between back pressure type generating set and condensing-type generating set.
As the vacuum method salt manufacturing of one of crude salt mode of production, mostly combine with fuel-burning power plant, utilize the malleation steam that back pressure type generating set or bleeder generating set are discharged to adopt multiple-effect cryogenic vacuum evaporation technology to produce crude salt, the feature of this technique is: although steam latent heat is fully utilized, generating efficiency is lower.
There is more producer to adopt seawater as water coolant near coastal fuel-burning power plant, its type of cooling can be divided into single flow and circulating, single flow refers to that seawater directly drains after the heat of cooling and absorbing generating set steam, after the circulating heat that refers to cooled with seawater absorption generating set steam, send into water cooling tower, after water cooling tower cooling, recycle, due to concentrating of water cooling tower, salinity improves constantly, and therefore needs timing to discharge denseer seawater, supplements into fresh seawater simultaneously.No matter which kind of mode is used seawater, and composition useful in its seawater is not effectively utilized.
The vapor temperature of its discharge of condensing-type generating set and steam-extracting type generating set (below take condensing-type generating set as example) is generally no more than 50 ℃ summer, and the winter in the north can be lower.The steam that steam turbine the is discharged water-cooled that is cooled is congealed into after water and is returned to boiler systems, and therefore the contained heat energy of this part steam is not utilized effectively.
Summary of the invention
For the deficiencies in the prior art, the object of the present invention is to provide a kind of heat utilization rate is high, seawater can get utilization condensing steam turbine generator group electricity, water, salt joint process.
The present invention is achieved by the following technical solutions:
Condensing steam turbine generator group electricity, water, salt joint process, its special character is to comprise the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thereby can generate electricity, be to enter interchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with the heat-eliminating medium heat exchange of extracting out from basin by forced circulation pump, tail steam is condensed into water, carries out returning to the use of boiler water processing systemic circulation after vapor-liquid separation in block steam and drain water device;
(2) heat-eliminating medium (temperature is above the boiling point) after heated enters vapour liquid separator, concentrate owing to isolating steam, in the time that in isolated liquid, salt concn reaches 300g/l～310g/l, part liquid is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine through forced circulation pump, and rest part is sent into interchanger after mixing with the heat-eliminating medium newly supplementing into and recycled;
(3) enter surface condenser from the isolated secondary steam of vapour liquid separator, fresh seawater through purifying treatment is added water cooling tower, be pumped into surface condenser by recirculated cooling water, with secondary steam heat exchange, secondary steam is condensed into fresh water and delivers to water pipe network, taken away by vacuum pump from surface condenser non-condensable gas out, absorb circulating cooling seawater reflux after heat to water cooling tower, after cooling, send again surface condenser to recycle with newly adding after the fresh seawater through purifying treatment of coming in is mixed;
Described heat-eliminating medium is bittern or Industry Waste salt solution;
Described heat-eliminating medium be through seawater refining system refining, from the circulating cooling seawater of water cooling tower.
Condensing steam turbine generator group electricity of the present invention, water, salt joint process, technique is simple, can realize electricity, salt, water coproduction, if combined with sea water desalinating plant, chlor-alkali (or soda ash) production equipment, not only can greatly alleviate environmental pollution, accomplish utilization of waste as resource, and can supply high-quality fresh water outward, greatly improve energy utilization rate, take full advantage of the negative pressure steam that enthalpy is lower, with less generating efficiency loss, get high-quality fresh water and industrial salt in return, the fresh water that only obtained is worth the value just reducing higher than loss generating.
Accompanying drawing explanation
Fig. 1: condensing steam turbine generator group electricity of the present invention, water, salt joint process schema;
In figure: 1, condensing steam turbine generator group, 2, interchanger, 3, block steam and drain water device, 4, boiler water processing system, 5, vapour liquid separator, 6, forced circulation pump, 7, chlor-alkali or soda ash system, 8, forced circulation pump, 9, basin, 10, surface condenser, 11, vacuum pump, 12, water pipe network, 13, water cooling tower, 14, circulating cooling water pump, 15, seawater refining system.
Embodiment
Further illustrate method provided by the present invention below in conjunction with accompanying drawing, but the present invention is not therefore subject to any restriction.
Condensing steam turbine generator group electricity, water, salt joint process, comprise the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thereby can generate electricity, be to enter interchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with the heat-eliminating medium heat exchange of extracting out from basin by forced circulation pump, tail steam is condensed into water, carries out returning to the use of boiler water processing systemic circulation after vapor-liquid separation in block steam and drain water device;
(2) heat-eliminating medium (temperature is above the boiling point) after heated enters vapour liquid separator, concentrate owing to isolating steam, in the time that in isolated liquid, salt concn reaches 300g/l～310g/l, part liquid is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine through forced circulation pump, and rest part is sent into interchanger after mixing with the heat-eliminating medium newly supplementing into and recycled;
(3) enter surface condenser from the isolated secondary steam of vapour liquid separator, fresh seawater through purifying treatment is added water cooling tower, be pumped into surface condenser by recirculated cooling water, with secondary steam heat exchange, secondary steam is condensed into fresh water and delivers to water pipe network, taken away by vacuum pump from surface condenser non-condensable gas out, absorb circulating cooling seawater reflux after heat to water cooling tower, after cooling, send again surface condenser to recycle with newly adding after the fresh seawater through purifying treatment of coming in is mixed;
Described heat-eliminating medium be through seawater refining system refining, from the circulating cooling seawater of water cooling tower.
The present embodiment is first by refining through seawater refining system, circulating cooling seawater from water cooling tower carrys out as heat-eliminating medium the steam that cooling steam turbine is discharged, after steam heating seawater, itself is condensed into water, in block steam and drain water device, carry out returning to the use of boiler water processing systemic circulation after vapor-liquid separation, after Absorption by Sea Water heat, temperature raises, the seawater that temperature exceedes after boiling point removes vapour liquid separator, the secondary steam of separating removes surface condenser, become fresh water to remove water pipe network by the circulating cooling seawater condensing from water cooling tower, contained non-condensable gas is taken away by vacuum pump, seawater after vapor-liquid separation is extracted out by forced circulation pump, after reaching 300g/l～310g/l, salt concn in seawater becomes the liquid brine that salts contg is qualified, extract a part of refined brine out and send chlor-alkali production system or soda ash production system as raw material salt solution, rest part continues circulating-heating with the sea water mixing of supplementing into, concentrated production liquid brine.
The kind of water cooling tower can be selected existing any form such as open type, enclosed and technology, make circulating cooling seawater reduce temperature by the mode of transpiring moisture, along with the evaporation of moisture, salt concn raises gradually, add from the seawater of circulating cooling system extraction some amount and remove to produce refined brine, therefore need constantly in system, to supplement fresh seawater.
Supplement into the seawater in water cooling tower and need carry out purifying treatment, in case water cooling tower fouling.
Interchanger can adopt any type of interchanger, the preferred shell and tube of interchanger or plate-type heat exchanger.Along with the carrying out of heat exchange, brine temp raises.When NaCl content in salt solution is when in 310g/l, vapour liquid separator, gaseous pressure is for-0.08MPa (gauge pressure), the about 67 ℃ of left and right of salt solution just come to life, under normal circumstances, salt solution saltiness is low, the boiling point lowering of salt solution, vacuum up, salt water boiling point also reduces, when NaCl content in salt solution is 310g/l, when be increased to-0.09MPa of vacuum tightness (gauge pressure), approximately 52 ℃ of salt solution will seethe with excitement.
Block steam and drain water device can adopt any type of block steam and drain water device, to reach the object that only allows liquid water to discharge and not allow steam to discharge.
Vapour liquid separator can adopt any type of vapor-liquid separating device, to reach the object of vapor-liquid separation.
Interchanger and vapour liquid separator also can adopt unitized, such as: levin evaporator, standard pan etc.
The mode vacuumizing can be mechanical type, can be also hydrojet formula.
Seawater circulating cooling mode and existing technique are basic identical, difference is in existing process of circulation cooling water, along with the operation of producing, in refrigerated sea water, the cycles of concentration of salt will progressively increase, therefore, require timing outside cooling system, to discharge the denseer seawater of a part, in case cooling system fouling, need constantly to supplement fresh seawater toward circulating cooling system, to guarantee system stable operation simultaneously.Feature of the present invention is from circulating cooling system, to extract continuously the denseer seawater of part out, be transferred to next step and go to produce the liquid brine that salt concentration is qualified, in the interior system of water cooling tower, supplement fresh seawater continuously, supplementary seawater amount is determined by the amount of producing the needed seawater amount of refined brine and water cooling tower transpiring moisture simultaneously.
The steam of discharging from steam turbine end is different from existing condensing steam turbine generator technique with temperature.The steam that existing condensing steam turbine generator end is discharged directly removes surface condenser, by the recirculated water cooling liquid water that congeals into, condensed water is returned to boiler water processing system again, the vapor temperature of discharge is generally no more than 50 ℃ summer, the negative pressure of its generation, in the case of the heat interchanging area of surface condenser is certain, mainly determines by quantity and the temperature of recirculated cooling water, under the certain condition of water coolant quantity, coolant water temperature is lower, and vacuum tightness is higher.The present invention is that the steam that condensing steam turbine is discharged is first sent interchanger to, heating comes self-circulation cooling system and treated seawater, the water condensing into returns to boiler water processing system after block steam and drain water device again, exhaust temperature is generally greater than 65 ℃, be less than 100 ℃, the negative pressure of its generation, in the situation that heat interchanging area is certain, mainly determines by quantity and the temperature of heated salt solution, control vapor temperature preferably≤85 ℃.
Seawater is in hydronic process, and the salt concn in secondary steam pressure and salt solution that its boiling point is mainly discharged by vapour liquid separator determines, and the pressure of secondary steam determines (being equivalent to technique and the technology of existing generating set) by surface condenser.Brine concentration is lower, and boiling point is lower.Under the certain condition of brine concentration, secondary steam pressure lower (that is: vacuum tightness is higher), the boiling point of salt solution is lower, thus vapor pressure and temperature that Steam Turbine is discharged are lower, and generating efficiency is just higher.Must control be in process of production not less than-0.08MPa of secondary steam vacuum tightness, (vacuum tightness is more high better), in finished product salt solution, NaCl content is 300g/1～310g/l, if lower than this scope, must continue circulating-heating concentrated, height goes beyond the scope, and must strengthen qualified salt solution extracted amount.
Take out seawater from circulating cooling system and go the mode of producing salt solution can adopt the mode of directly sending outside from cooling-water pump, a water pump also can be installed separately and specialize in production salt solution.
Can be treated from strong brine, bittern etc. after seawater, the sea water desaltination of water cooling tower circulating cooling system for the production of the raw material (heat-eliminating medium) of refined brine, also can be the brine waste of producing epoxy chloropropane, MDI and other products by-product, or ionic membrane method produces the dechlorination light salt brine in caustic soda process, or combination between them and supplementing.But, no matter what does raw material with, must guarantee that all raw materials must not produce fouling (with water cooling tower circulating cooling system) after heating is concentrated, concrete processing mode (such as ion-exchange-resin process etc.) the present invention is not discussed.
The present invention, except can production liquid brine, can also install by increase the mode production solid state crystallization salt of crystallizer.
The present invention can separate use by water cooling tower circulating cooling system and steam turbine exhaust vapour heating concentration systems, that is: existing water cooling tower process of circulation cooling water is constant, the concentrated production liquid brine of negative pressure steam heating of discharging with turbine driven set steam turbine separately.
The unspecified content of the present invention is prior art, and those skilled in the art can obtain inspiration from the present embodiment and prior art, is out of shape and obtains other embodiment.Therefore, protection scope of the present invention should be determined according to the protection domain of claim.
Claims (3)
1. condensing steam turbine generator group electricity, water, salt joint process, is characterized in that comprising the following steps:
(1) the Steam Actuation condensing steam turbine generator group running that upper level technique produces, thereby can generate electricity, be to enter interchanger lower than the tail steam of-0.04MPa from condensing steam turbine generator group gauge pressure out, with the heat-eliminating medium heat exchange of extracting out from basin by forced circulation pump, tail steam is condensed into water, carries out returning to the use of boiler water processing systemic circulation after vapor-liquid separation in block steam and drain water device;
(2) heat-eliminating medium (temperature is above the boiling point) after heated enters vapour liquid separator, concentrate owing to isolating steam, in the time that in isolated liquid, salt concn reaches 300g/l～310g/l, part liquid is extracted out and is delivered to chlor-alkali or soda ash production system as qualified refined brine through forced circulation pump, and rest part is sent into interchanger after mixing with the heat-eliminating medium newly supplementing into and recycled;
(3) enter surface condenser from the isolated secondary steam of vapour liquid separator, fresh seawater through purifying treatment is added water cooling tower, be pumped into surface condenser by recirculated cooling water, with secondary steam heat exchange, secondary steam is condensed into fresh water and delivers to water pipe network, taken away by vacuum pump from surface condenser non-condensable gas out, absorb circulating cooling seawater reflux after heat to water cooling tower, after cooling, send again surface condenser to recycle with newly adding after the fresh seawater through purifying treatment of coming in is mixed.
2. condensing steam turbine generator group electricity, water, salt joint process according to claim 1, is characterized in that described heat-eliminating medium is bittern or Industry Waste salt solution.
3. condensing steam turbine generator group electricity, water, salt joint process according to claim 1, it is characterized in that described heat-eliminating medium be through seawater refining system refining, from the circulating cooling seawater of water cooling tower.
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| CN201310729374.2A CN103787434B (en) | 2013-12-19 | 2013-12-19 | Condensing steam turbine generator group electricity, water, salt joint production process |
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| CN201310729374.2A CN103787434B (en) | 2013-12-19 | 2013-12-19 | Condensing steam turbine generator group electricity, water, salt joint production process |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105314655A (en) * | 2015-10-19 | 2016-02-10 | 中盐榆林盐化有限公司 | Method and device for utilizing brine geothermal energy and condensed water heat energy |
| CN105923873A (en) * | 2016-05-26 | 2016-09-07 | 潘庆光 | Treatment method of exhausted salty water produced through isocyanate ester production system |
| CN107796237A (en) * | 2017-11-30 | 2018-03-13 | 无锡弘鼎华化工设备有限公司 | negative pressure steam heating method and system |
| CN107823909A (en) * | 2017-10-23 | 2018-03-23 | 张家港市江南锅炉压力容器有限公司 | A kind of reboiler for destilling tower |
| CN110926049A (en) * | 2019-12-05 | 2020-03-27 | 陕西鼓风机（集团）有限公司 | Cogeneration low-temperature heating process and system |
| CN114922699A (en) * | 2022-05-11 | 2022-08-19 | 首钢京唐钢铁联合有限责任公司 | Cooling system of boiler steam turbine generator unit and control method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105314655A (en) * | 2015-10-19 | 2016-02-10 | 中盐榆林盐化有限公司 | Method and device for utilizing brine geothermal energy and condensed water heat energy |
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| CN105923873A (en) * | 2016-05-26 | 2016-09-07 | 潘庆光 | Treatment method of exhausted salty water produced through isocyanate ester production system |
| CN105923873B (en) * | 2016-05-26 | 2018-12-18 | 潘庆光 | A kind of processing method for the effluent brine that carbimide production system generates |
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| CN110926049A (en) * | 2019-12-05 | 2020-03-27 | 陕西鼓风机（集团）有限公司 | Cogeneration low-temperature heating process and system |
| CN110926049B (en) * | 2019-12-05 | 2023-11-21 | 陕西鼓风机（集团）有限公司 | Cogeneration low-temperature heating process and system |
| CN114922699A (en) * | 2022-05-11 | 2022-08-19 | 首钢京唐钢铁联合有限责任公司 | Cooling system of boiler steam turbine generator unit and control method |
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| Publication number | Publication date |
|---|---|
| CN103787434B (en) | 2016-05-18 |
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