CN113044919A - Fine treatment process and device for condensed water in power plant - Google Patents
Fine treatment process and device for condensed water in power plant Download PDFInfo
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- CN113044919A CN113044919A CN202110469549.5A CN202110469549A CN113044919A CN 113044919 A CN113044919 A CN 113044919A CN 202110469549 A CN202110469549 A CN 202110469549A CN 113044919 A CN113044919 A CN 113044919A
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- ion exchanger
- pipeline
- bed ion
- exchange resin
- cation
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 227
- 238000000034 method Methods 0.000 title claims abstract description 33
- 150000002500 ions Chemical class 0.000 claims abstract description 221
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 152
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 152
- 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 claims abstract description 109
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 74
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 74
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 61
- 238000011069 regeneration method Methods 0.000 claims abstract description 56
- 230000008929 regeneration Effects 0.000 claims abstract description 55
- 239000003729 cation exchange resin Substances 0.000 claims abstract description 35
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 23
- 238000005406 washing Methods 0.000 claims abstract description 12
- 238000011001 backwashing Methods 0.000 claims abstract description 9
- 150000001768 cations Chemical class 0.000 claims description 99
- 150000001450 anions Chemical class 0.000 claims description 55
- 238000005342 ion exchange Methods 0.000 claims description 36
- 239000007788 liquid Substances 0.000 claims description 20
- 238000005498 polishing Methods 0.000 claims description 20
- 239000002699 waste material Substances 0.000 claims description 18
- 238000002360 preparation method Methods 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 11
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 11
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- 239000011734 sodium Substances 0.000 claims description 11
- 229910052708 sodium Inorganic materials 0.000 claims description 11
- 230000001172 regenerating effect Effects 0.000 claims description 10
- 238000005341 cation exchange Methods 0.000 claims description 8
- 238000011033 desalting Methods 0.000 claims description 8
- 238000007517 polishing process Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000005349 anion exchange Methods 0.000 claims description 6
- 238000007670 refining Methods 0.000 claims description 2
- 239000002253 acid Substances 0.000 abstract description 3
- 239000012492 regenerant Substances 0.000 abstract description 3
- 239000003513 alkali Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 238000009833 condensation Methods 0.000 description 8
- 230000005494 condensation Effects 0.000 description 8
- 238000002156 mixing Methods 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- 239000000908 ammonium hydroxide Substances 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000001727 in vivo Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- 239000012736 aqueous medium Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000000338 in vitro Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
- B01J49/53—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for cationic exchangers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/50—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents
- B01J49/57—Regeneration or reactivation of ion-exchangers; Apparatus therefor characterised by the regeneration reagents for anionic exchangers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/60—Cleaning or rinsing ion-exchange beds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
- C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
Abstract
The invention discloses a fine treatment process and a fine treatment device for condensed water in a power plant, belonging to the technical field of water treatment; the process comprises the following steps: (1) and (3) treating condensed water: finely processing the condensed water by using ion exchange resin regenerated by ammonia water; (2) backwashing the ion exchange resin; (3) ion exchange resin regeneration: regeneration of spent ion exchange resin, NH in aqueous ammonia using aqueous ammonia4 +Regenerated cation exchange resin, OH－Regenerating the anion exchange resin; (4) and (5) direct washing. The ion exchange resin which is out of work when the process and the device are used for carrying out the fine treatment of the condensed water of the power plantThe ion exchanger does not need to be unloaded, and the ion exchanger does not need to be separated into cation exchange resin and anion exchange resin, so that the system structure and the operation process are simplified, and the technical difficulty is reduced; meanwhile, the water quality pollution of acid and alkali regenerant residual substances used in the conventional ion exchange resin regeneration process to a steam-water system of a thermal power plant is avoided, and the steam-water quality of the thermal power plant is improved.
Description
Technical Field
The invention relates to the technical field of water treatment, in particular to a process and a device for finely treating condensed water in a power plant.
Background
In the thermal power factory, the unit that capacity is greater than 300MW generally is equipped with the condensate fine treatment system for get rid of the impurity ion in the condensate, purify the condensate. The condensate fine treatment system is key equipment for ensuring qualified water quality of a steam-water system of a thermal power plant and safe operation of a unit, and a plurality of technical problems which are difficult to solve exist in the prior art and operation:
1. in order to improve the ion exchange treatment effect, an H/OH mixed bed ion exchange treatment process is adopted; during the treatment of the condensed water, ammonium hydroxide used for adjusting the pH of the condensed water is exchanged and absorbed by the mixed ion exchange resin, resulting in: firstly, the mixed ion exchange resin has short operation period and quick failure; secondly, the pH value of the treated condensed water is low, and ammonia water (ammonium hydroxide) is added to increase the pH value of the condensed water.
2. After the mixed ion exchange resin is failed, the ion exchanger is unloaded, the mixed ion exchange resin is separated into cation exchange resin and anion exchange resin, the cation exchange resin and the anion exchange resin are respectively regenerated by another ion exchange resin regeneration device, and the regenerated cation exchange resin and anion exchange resin are remixed by the mixing device to form the mixed ion exchange resin which is loaded into the mixed bed ion exchanger for use. Therefore, the existing condensate polishing system is complex, the technical requirement of the operation process is high, and especially the mixed ion exchange resin can not achieve complete separation at present; the method is difficult to overcome by the existing treatment process of the condensed water of the power plant.
3. The mixed ion exchange resin is worn due to frequent operations of loading, unloading, separating, conveying, mixing and the like, so the condensate polishing system must use the ion exchange resin with special performance, and has high price and high running cost.
4. H in HCl used in mixed bed ion exchange process for treating H/OH+Regenerating the cation exchange resin with Cl－Entering regenerated waste liquid; using OH in NaOH－Regenerating the anion exchange resin while Na+Entering regenerated waste liquid; resulting in: (ii) Cl－And Na+Environmental pollution by the discharge of regenerated waste liquid, in which Cl is contained－Leading to the difficulty in the treatment and the recycling of the waste water of the thermal power plant; ② to preventCl－And Na+The ion exchange resin of the condensate polishing device must be regenerated in vitro, which causes the condensate polishing device to have complicated and large equipment and difficult operation.
5. The condensate polishing device is operated from H/OH operation state to NH4 +The conversion of the/OH operating state needs to be carried out under conditions of good water quality of the condensed water, high regeneration degree of the ion exchange resin and high purity of HCl and NaOH regenerants. These conditions are difficult to satisfy at present on-site operation conditions, so that currently, a condensate treatment device NH is realized4 +The case of the/OH run is very rare.
6. The incomplete separation of the mixed ion exchange resin causes the pollution of condensed water in the operation process of a condensed water fine treatment system.
Therefore, how to provide a condensate polishing process and a condensate polishing device which have simple structure and convenient operation and can effectively improve the quality of the steam water of the thermal power plant is a technical problem to be solved in the field.
Disclosure of Invention
In view of the above, the present invention provides a condensate polishing process and apparatus for a power plant, which has a simple structure and is convenient to operate, and can improve the condensate polishing efficiency.
In order to achieve the purpose, the invention adopts the following technical scheme:
a power plant condensate polishing process comprises the following steps:
(1) and (3) treating condensed water: refining the condensed water by using ion exchange resin regenerated by ammonia water, wherein Fe in the condensed water3+、Na+、Cl－And SO4 2－Conversion of ions to NH by cation exchange and anion exchange4 +And OH－；
(2) Ion exchange resin backwashing: after the ion exchange resin is invalid, backwashing by using desalted water;
(3) ion exchange resin regeneration: regeneration of spent ion exchange resin, NH in aqueous ammonia using aqueous ammonia4 +Regenerated cation exchange resin, OH－Regeneration anionA sub-exchange resin;
(4) washing in a normal way: the regenerated ion exchange resin was washed with demineralized water.
The condensed water is finely treated by using ion exchange resin regenerated by ammonia water, and the condensed water is finely treated and directly enters NH4 +The operation condition of/OH avoids the prior art from shifting from the operation condition of H/OH to NH4 +The water quality generated in the process of the/OH operation working condition is deteriorated, and the operation period of the ion exchange resin is prolonged.
Regenerating by ammonia water after the ion exchange resin is invalid, wherein NH in the ammonia water4 +Regenerating the cation exchange resin: RFe + RNA + NH4 +→RNH4CFe3++Na+，OH－Regenerated anion exchange resin RCl + RSO4+OH－→ROH+Cl－+SO4 2－(ii) a NH when the regenerated ion exchange resin is used for treating condensed water4 +And OH－And releasing the condensate into the condensate to adjust the pH value of the condensate: cation exchange equation: RNH4+Fe3++Na+→RFe+RNa+NH4 +The anion exchange equation: ROH + Cl－+SO4 2－→RCl+RSO4+OH－(ii) a Namely, the ammonia water plays the dual roles of regenerating ion exchange resin and adjusting the pH value of condensed water at the same time, thereby saving acid and alkali regenerants, and avoiding the regenerants HCl and NaOH from regenerating residual Cl－And Na+The quality of the steam and water of the generator set is influenced, and the environmental pollution is reduced.
After the ion exchange resin is invalid, the ammonia water is directly used for in vivo regeneration, the ion exchanger does not need to be unloaded, the mixed ion exchange resin does not need to be separated into cation exchange resin and anion exchange resin, HCl and NaOH do not need to be used for respectively regenerating the cation exchange resin and the anion exchange resin, the operations of loading, unloading, separating, conveying, mixing and the like of the ion exchange resin do not need to be repeatedly carried out, the abrasion of the ion exchange resin is small, the special ion exchange resin with abrasion resistance and high price does not need to be used, the condensate polishing system and the operation are simplified, and the equipment investment and the operation cost are reduced; and the pollution of condensed water in the process of fine treatment and operation of the condensed water caused by incomplete separation of the mixed ion exchange resin is avoided.
Further, after the step (4), the ion exchange resin is continuously used for the step (1) of treating the condensed water.
Preferably, when the mixed bed ion exchanger is used as an ion exchange system of a condensate polishing device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and regeneration requirements (such as regeneration specific consumption and regeneration degree);
secondly, ammonia water enters the mixed bed ion exchanger, and cation exchange resin and anion exchange resin in the mixed ion exchange resin are regenerated at the same time;
thirdly, introducing desalted water according to the same flow rate and flow-through way as the ammonia water after the prepared ammonia water is used, and replacing regenerated waste liquid and residual ammonia water in the mixed bed ion exchanger; after the replacement, the regeneration process is completed.
Preferably, when the preposed cation bed ion exchanger + mixed bed ion exchanger is adopted as the ion exchange system of the condensate polishing device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters the mixed bed ion exchanger, and cation exchange resin and anion exchange resin in the mixed ion exchange resin are regenerated at the same time; then enters a preposed cation bed ion exchanger, and residual NH in the regenerated liquid is discharged by utilizing the mixed bed ion exchanger4 +Regenerating the cation exchange resin;
thirdly, introducing desalted water according to the same flow rate and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the mixed bed ion exchanger and the pre-cation bed ion exchanger; after the replacement, the regeneration process is completed.
Preferably, when a cation bed ion exchanger + an anion bed ion exchanger or an anion bed ion exchanger + a cation bed ion exchanger is employed as the ion exchange system of the condensed water fine treatment apparatus,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters an anion bed ion exchanger and an anion bed ion exchanger in sequence, or enters an anion bed ion exchanger and an cation bed ion exchanger in sequence, cation exchange resin is regenerated in the cation bed ion exchanger, and anion exchange resin is regenerated in the anion bed ion exchanger;
thirdly, introducing desalted water according to the same flow velocity and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the cation bed ion exchanger and the anion bed ion exchanger; after the replacement, the regeneration process is completed.
Further preferably, during operation, the condensed water can firstly pass through the cation bed ion exchanger, can also firstly pass through the anion bed ion exchanger, and can avoid Fe in the condensed water by firstly passing through the cation bed ion exchanger3+Anion exchange resin which is difficult to recover; during regeneration, the ammonia water can firstly pass through the cation bed ion exchanger or the anion bed ion exchanger, but after the cation exchange resin is regenerated by the cation bed ion exchanger, NH in the ammonia water4OH is converted into NaOH with stronger alkalinity, which is beneficial to improving the subsequent regeneration effect of the anion exchange resin.
Preferably, when the pre-cation bed ion exchanger + anion bed ion exchanger or the pre-cation bed ion exchanger + anion bed ion exchanger + cation bed ion exchanger is used as the ion exchange system of the condensed water fine treatment device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters an anion bed ion exchanger and an anion bed ion exchanger in sequence, or enters an anion bed ion exchanger and an cation bed ion exchanger in sequence, cation exchange resin is regenerated in the cation bed ion exchanger, and anion exchange resin is regenerated in the anion bed ion exchanger; finally, the cation exchange resin enters a preposed cation bed ion exchanger to regenerate cation exchange resin;
thirdly, introducing desalted water according to the same flow rate and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the cation bed ion exchanger, the anion bed ion exchanger and the preposed cation bed ion exchanger; after the replacement, the regeneration process is completed.
Preferably, the flow direction of the ammonia water passing through the ion exchanger in the step (3) is the same as the flow direction of the condensed water passing through the ion exchanger in the step (1) (concurrent flow regeneration) or opposite (countercurrent flow regeneration), and the quality of the effluent water treated by the condensed water in a countercurrent flow regeneration mode is better.
A power plant condensed water fine treatment device comprises an ammonia water preparation system, an ion exchange system, a condensed water inflow pipeline and a condensed water outflow pipeline;
the ammonia water preparation system comprises an ammonia water tank, a mixer, a circulating booster pump, a desalting water tank and a liquid ammonia tank;
the ammonia tank, the mixer and the circulating booster pump are mutually connected through pipelines to form a circulating loop;
the desalting water tank is connected to a pipeline between the ammonia water tank and the circulating booster pump through a pipeline;
the liquid ammonia tank is connected with the mixer through a pipeline;
the ion exchange system is connected to a pipeline between the mixer and the circulating booster pump through a pipeline;
the condensed water inflow pipeline and the condensed water outflow pipeline are respectively connected with the ion exchange system.
Form circulation circuit through the pipeline between ammonia jar, blender and the circulation booster pump, the liquid ammonia jar passes through the tube coupling blender for when dissolving liquid ammonia in the demineralized water, circulation demineralized water (or weak ammonia water) and liquid ammonia direct mixing have avoided in the traditional handicraft to prepare the strong sound of device and vibration that the process aqueous ammonia is exothermic in a large number and leads to in process aqueous ammonia. The desalted water (or dilute ammonia water) is mixed with the liquid ammonia in the circulating flow process, which is beneficial to preparing the ammonia water with higher concentration accuracy. Liquid ammonia and demineralized water (or weak ammonia water) direct contact dissolve, save the relevant indirect heating equipment of two steps of liquid ammonia gasification heating and gas ammonia solution cooling or part of traditional aqueous ammonia preparation in-process, simplify the structure, reduce the energy consumption. The condensed water inflow pipeline and the condensed water outflow pipeline are respectively connected with the ion exchange system, the ion exchange system is connected on a pipeline between the mixer and the circulating booster pump through a pipeline, the ion exchange resin can be regenerated in vivo after being out of service, the condensed water treatment can be continued after the regeneration, and the operation is convenient; the existing power plant condensate fine treatment device can be directly transformed into the novel power plant condensate fine treatment device through the condensate inflow pipeline and the condensate outflow pipeline, and the engineering investment of the invention is reduced.
Preferably, the ion exchange system comprises one or more sets of ion exchangers,
each group of ion exchangers is any one of the following:
firstly, a mixed bed ion exchanger;
② a front cation bed ion exchanger and a mixed bed ion exchanger;
③ cation bed ion exchanger and anion bed ion exchanger;
fourthly, a front cation bed ion exchanger, a cation bed ion exchanger and an anion bed ion exchanger are arranged;
(v) anion bed ion exchanger + cation bed ion exchanger;
sixthly, the preposed cation bed ion exchanger, the anion bed ion exchanger and the cation bed ion exchanger.
The invention omits a large amount of devices such as a mixed ion exchange resin separation device, an ion exchange resin mixing and storing device and the like, and simplifies a condensed water mixed bed fine treatment device.
The ion exchange system is added with a front cation bed ion exchanger. During operation, the condensed water passes through the ion exchanger of the front anode bed to remove Fe in the condensed water through cation exchange3+And part of Na+Isocationizing, and removing C l by ion exchanger－、SO4 2－Plasma anion and residual Na+An isocationic acid; during regeneration, the ammonia water regenerant firstly passes through other ion exchangers to regenerate the ion exchange resin, then enters the front cation bed ion exchanger, and utilizes other ion exchangersDischarging residual NH in the regeneration waste liquid4 +The cation exchange resin in the preposed cation bed ion exchanger is regenerated, the utilization rate of the ammonia water is high, and NH in the ammonia water regenerant is avoided4 +The waste liquid is discharged along with the regeneration to pollute the environment.
Further preferably, the cation exchanger of the pre-anode bed uses a weakly acidic cation exchange resin. In the basic aqueous medium of the condensed water, the weakly acidic cation exchange resin has a larger ion exchange capacity than the strongly acidic cation exchange resin.
Preferably, a condensed water flow meter is arranged on the condensed water inflow pipeline;
the condensed water outlet pipeline is provided with a hydrogen conductivity meter and a sodium meter for monitoring whether the quality of the water treated by the ion exchange system reaches the quality limit index of the condensed water treatment, and then judging whether the condensed water treatment needs to be stopped, and performing ion exchange resin regeneration.
Preferably, a conductivity meter and an ammonia water flowmeter are arranged on a pipeline between the ammonia water tank and the circulating booster pump.
Preferably, each pipeline can be provided with a valve, and the flow direction of the ammonia water and the desalted water is changed and the sequence of introducing the ammonia water and the desalted water into different ion exchangers is changed according to the on-off of the valves.
Preferably, when the device is used for preparing ammonia water, firstly, desalted water in the brine tank flows into the ammonia water tank through the circulating booster pump and the mixer; when the water level of the ammonia water tank reaches the set water level of the desalted water required for preparing the ammonia water, stopping injecting the desalted water, and enabling the desalted water to circularly flow among the ammonia water tank, the circulating booster pump and the mixer; and mixing the liquid ammonia in the liquid ammonia tank with desalted water (or dilute ammonia water) by a mixer and then flowing into an ammonia water tank, wherein the prepared ammonia water circularly flows among the ammonia water tank, the circulating booster pump and the liquid ammonia mixer. With the continuous addition of liquid ammonia, the concentration of ammonia water in preparation and the corresponding conductivity are continuously improved; and when the conductivity of the prepared ammonia water reaches a set conductivity value, the ammonia water is prepared for standby.
In conclusion, the invention simplifies the structure and the operation process of the condensate fine treatment system of the power plant, is beneficial to improving the quality of the condensate and is suitable for popularization and application.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic structural diagram of an apparatus according to embodiment 1 of the present invention.
FIG. 2 is a schematic view of the piping connection of the apparatus according to embodiment 1 of the present invention.
FIG. 3 is a schematic structural diagram of an apparatus according to embodiment 2 of the present invention.
FIG. 4 is a schematic view of the piping connection of the apparatus according to embodiment 2 of the present invention.
FIG. 5 is a schematic structural diagram of an apparatus according to embodiment 3 of the present invention.
FIG. 6 is a schematic view of the piping connection of the apparatus according to embodiment 3 of the present invention.
FIG. 7 is a schematic diagram of the structure of an apparatus according to embodiment 4 of the present invention.
FIG. 8 is a schematic view of the piping connection of the apparatus according to embodiment 4 of the present invention.
Reference numerals:
11. an ammonia tank; 12. a mixer; 13. a circulating booster pump; 14. a demineralized water tank; 15. a liquid ammonia tank;
101. a first pipeline; 102. a second pipeline; 1021. a second pipeline valve; 103. a third pipeline; 1031. a pipeline three valve; 1032. a conductivity meter; 1033. an ammonia flowmeter; 104. a fourth pipeline; 1041. a pipeline four valve; 105. a fifth pipeline; 1051. a pipeline five valve; 106. a sixth pipeline; 1061. a pipeline six-valve;
21. a mixed bed ion exchanger; 201. a mixed bed ion exchanger pipeline I; 202. a mixed bed ion exchanger pipeline II; 203. a branch pipeline I; 2031. a valve of the branch pipeline; 204. a branch pipeline II; 2041. a branch pipeline two valve; 205. a branch pipeline III; 2051. a branch pipeline three valve; 206. a branch pipeline IV; 2061. a branch pipeline four-valve; 207. a seventh pipeline; 2071. a pipeline seven valve;
22. a front cation bed ion exchanger; 221. a first pipeline of the preposed cation bed ion exchanger; 222. a second preposed cation bed ion exchanger pipeline; 223. a branch pipeline five; 2231. a branch pipeline five valve; 224. a branch pipeline six; 2241. a branch pipeline six valve; 225. a branch pipeline seven; 2251. a branch pipeline seven valve; 226. a branch pipeline eight; 2261. eight valves of branch pipelines; 227. a branch line nine; 2271. a branch pipeline nine is provided with a first valve; 2272. a branch pipeline nine valve II; 228. a branch line twenty; 2281. a branch pipeline twenty valves I; 2282. a branch pipeline twenty valves II; 229. a branch pipeline II; 2291. a branch pipeline II and a branch pipeline I are connected; 2292. a branch pipeline II and a valve II;
23. an anion bed ion exchanger; 231. a first anion exchanger pipeline; 232. a second anion exchanger pipeline; 233. ten branch pipelines; 2331. a branch pipeline ten-valve; 234. eleven branch lines; 2341. eleven valves of branch pipelines; 235. a branch line twelve; 2351. a branch pipeline twelve valve one; 2352. a branch pipeline twelve valve II; 236. a branch line thirteen; 2361. a branch pipeline thirteen valve I; 2362. a branch pipeline thirteen valve II; 237. a branch line fourteen; 2371. a branch pipeline fourteen-valve; 238. a branch line fifteen; 2381. a branch line fifteen-valve;
24. cation bed ion exchangers; 241. a cation bed ion exchanger pipeline I; 242. a cation bed ion exchanger pipeline II; 243. sixteen branch pipelines; 2431. sixteen valves of branch pipelines; 244. a branch line seventeen; 2441. a branch line seventeen valve; 245. eighteen branch lines; 2451. eighteen valves of branch pipelines; 246. nineteen branch pipelines; 2461. a branch line nineteen-valve;
31. a condensate inlet; 301. the condensed water flows into the pipeline; 3011. a condensate flowmeter; 3012. the condensed water flows into the pipeline valve;
41. a condensed water outlet; 401. the condensed water flows out of the pipeline; 4011. the condensed water flows out of the first pipeline valve; 4012. a hydrogen conductivity meter; 4013. a sodium meter; 4014. a second pipeline valve for condensed water to flow out;
5. and (4) digging a trench.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
As shown in fig. 1-2, a power plant condensate polishing apparatus includes an ammonia water preparation system, an ion exchange system, a condensate inflow pipe 301 and a condensate outflow pipe 401;
the ammonia water preparation system comprises an ammonia water tank 11, a mixer 12, a circulating booster pump 13, a desalting water tank 14 and a liquid ammonia tank 15;
the ammonia water tank 11 is connected with the mixer 12 through a first pipeline 101, the mixer 12 is connected with the circulating booster pump 13 through a second pipeline 102, and the circulating booster pump 13 is connected with the ammonia water tank 11 through a third pipeline 103;
the desalted water tank 14 is connected to the third pipeline 103 through the fourth pipeline 104;
the liquid ammonia tank 15 is connected to the mixer 12 through a line five 105.
A second pipeline 102 is provided with a second pipeline valve 1021;
a third pipeline 103 is provided with a third pipeline valve 1031, a conductivity meter 1032 and an ammonia water flow meter 1033;
a pipeline four valve 1041 is arranged on the pipeline four 104;
a fifth pipeline valve 1051 is arranged on the fifth pipeline 105;
a pipeline six 106 is branched from the pipeline two valve 1021 on the pipeline two 102 and the circulating booster pump 13, and a pipeline six valve 1061 is arranged on the pipeline six 106.
The ion exchange system comprises a mixed bed ion exchanger 21, wherein a mixed bed ion exchanger pipeline I201 and a mixed bed ion exchanger pipeline II 202 are respectively arranged at two ends of the mixed bed ion exchanger 21;
the first mixed bed ion exchanger pipe 201 is connected with a branch pipe 203 and a branch pipe 204,
a branch pipeline III 205, a branch pipeline IV 206 and a condensed water outlet pipeline 401 are connected to the mixed bed ion exchanger pipeline II 202;
the branch pipeline I203 is connected with the condensed water inflow pipeline 301;
the second branch pipe 204 and the fourth branch pipe 206 are converged and connected into the trench 5;
branch line three 205 connects line six 106.
A branch pipeline one valve 2031 is arranged on the branch pipeline one 203;
a branch line two valve 2041 is arranged on the branch line two 204;
a branch pipeline three valve 2051 is arranged on the branch pipeline three 205;
a branch line four valve 2061 is provided in the branch line four 206.
The condensation water inlet pipeline 301 is characterized by further comprising a pipeline seven 207, wherein one end of the pipeline seven 207 is connected to the junction of the branch pipeline one 203 and the condensation water inlet pipeline 301, and the other end of the pipeline seven is connected to the junction of the branch pipeline three 205 and the pipeline six 106; a seventh pipeline valve 2071 is disposed on the seventh pipeline 207.
One end of the condensed water inflow pipeline 301 is provided with a condensed water inlet 31, a condensed water flowmeter 3011 is arranged on the condensed water inflow pipeline 301, and a condensed water inflow pipeline valve 3012;
one end of the condensed water outlet pipeline 401 is a condensed water outlet 41, and a condensed water outlet pipeline valve I4011, a hydrogen conductivity meter 4012, a sodium meter 4013 and a condensed water outlet pipeline valve II 4014 are arranged on the condensed water outlet pipeline 401.
The device is used for carrying out condensate polishing, and comprises the following steps:
(1) and (3) treating condensed water:
the condensed water enters the mixed-bed ion exchanger 21 through a condensed water inlet 31, a condensed water flow meter 3011, a condensed water inflow pipeline valve 3012 and a branch pipeline-valve 2031 (the mixed ion exchange resin in the mixed ion exchanger is regenerated by ammonia water); in the mixed bed ion exchanger 21, Cl in the condensed water－、SO4 2－、Fe3+、Na+Removal by anion exchange and cation exchange, the cation exchange equation: RNH4+Fe3++Na+→RFe+RNa+NH4 +The anion exchange equation: ROH + Cl－+SO4 2－→RCl+RSO4+OH－The condensed water is purified; the purified condensed water is delivered to a steam-water system of a power plant unit through a condensed water outlet pipe valve II 4014, a sodium meter 4013, a hydrogen conductivity meter 4012 and a pipe valve I4011; when the hydrogen conductivity meter 4012 and the sodium degree meter 4013 show that the quality of the treated water of the mixed bed ion exchanger 21 approaches the quality limit index of the treated water of the condensed water, the operation process is finished.
(2) Ion exchange resin backwashing:
starting the circulating booster pump 13, enabling the demineralized water in the demineralized water tank 14 to enter the mixed bed ion exchanger 21 through the four pipeline valves 1041, the conductivity meter 1032, the ammonia water flow meter 1033, the circulating booster pump 13, the six pipeline valves 1061 and the three branch pipeline valves 2051, and backwashing the mixed ion exchange resin; backwash effluent is discharged into the trench 5 through a branch line valve 2041.
(3) Ion exchange resin regeneration:
preparing ammonia water: according to the quantity of the ion exchange resin to be regenerated and the regeneration requirement, presetting the volume and concentration of the prepared ammonia water, starting a circulating booster pump 13, and adding a preset quantity of demineralized water into an ammonia water tank 11 through a four-valve pipe 1041, a conductivity meter 1032, an ammonia water flow meter 1033, the circulating booster pump 13, a two-valve pipe 1021 and a mixer 12; then, the four valves 1041 of the pipeline are closed, the three valves 1031 of the pipeline are opened, and the demineralized water is circulated among the ammonia water tank 11, the mixer 12 and the circulating booster pump 13; slowly opening a five-valve 1051 of the pipeline, enabling liquid ammonia to enter a mixer 12, mixing and dissolving the liquid ammonia with demineralized water, enabling the liquid ammonia to enter an ammonia water tank 11, and circulating among the ammonia water tank 11, the mixer 12 and a circulating booster pump 13; and reading the conductivity value of the prepared ammonia water through a conductivity meter 1032, closing the five-pipeline valve 1051 when the conductivity value reaches a preset value, continuously running the circulating booster pump 13 for 10 minutes, and then closing the two-pipeline valve 1021, the circulating booster pump 13 and the three-pipeline valve 1031 in sequence to finish the preparation of the ammonia water.
Regeneration: starting the circulating booster pump 13 to make ammonia water pass through the three valve 1031 of the pipeline and the conductivityThe instrument 1032, the ammonia water flow meter 1033, the circulating booster pump 13, the six-valve 1061 of the pipeline and the three-valve 2051 of the branch pipeline enter the mixed bed ion exchanger 21, and simultaneously, cation exchange resin and anion exchange resin in the failed mixed ion exchange resin, NH in the ammonia water are regenerated4 +Regenerating the cation exchange resin: RFe + RNA + NH4 +→RNH4CFe3++Na+，OH－Regenerated anion exchange resin RCl + RSO4+OH－→ROH+Cl－+SO4 2－(ii) a The regenerated waste liquid discharged from the mixed bed ion exchanger 21 is discharged to the trench 5 through the branch line valve 2041.
And (3) replacement: after the ammonia water is used, opening the four-valve 1041 of the pipeline, closing the three-valve 1031 of the pipeline, and replacing the regenerated waste liquid and the residual ammonia water in the mixed bed ion exchanger 21 by the desalted water according to the way through which the ammonia water flows; after the replacement, the regeneration process is completed.
(4) Washing in a normal way:
closing the branch line three-valve 2051 and the branch line two-valve 2041, opening the pipeline seven-valve 2071, the branch line one-valve 2031 and the branch line four-valve 2061, allowing the demineralized water in the demineralized water tank 14 to enter the mixed bed ion exchanger 21 through the pipeline four-valve 1041, the conductivity meter 1032, the ammonia water flow meter 1033, the circulating booster pump 13, the pipeline six-valve 1061, the pipeline seven-valve 2071 and the branch line one-valve 2031 to forward wash the mixed ion exchange resin, discharging the forward wash water through the branch line four-valve 2061 to enter the trench 5, and finishing the forward washing process.
The four steps are circularly reciprocated, and the condensed water fine treatment device of the power plant continuously operates.
Example 2
As shown in fig. 3-4, a power plant condensate polishing apparatus includes an ammonia water preparation system, an ion exchange system, a condensate inflow pipe 301 and a condensate outflow pipe 401;
the ammonia water preparation system comprises an ammonia water tank 11, a mixer 12, a circulating booster pump 13, a desalting water tank 14 and a liquid ammonia tank 15;
the ammonia water tank 11 is connected with the mixer 12 through a first pipeline 101, the mixer 12 is connected with the circulating booster pump 13 through a second pipeline 102, and the circulating booster pump 13 is connected with the ammonia water tank 11 through a third pipeline 103;
the desalted water tank 14 is connected to the third pipeline 103 through the fourth pipeline 104;
the liquid ammonia tank 15 is connected to the mixer 12 through a line five 105.
A second pipeline 102 is provided with a second pipeline valve 1021;
a third pipeline 103 is provided with a third pipeline valve 1031, a conductivity meter 1032 and an ammonia water flow meter 1033;
a pipeline four valve 1041 is arranged on the pipeline four 104;
a fifth pipeline valve 1051 is arranged on the fifth pipeline 105;
a pipeline six 106 is branched from the pipeline two valve 1021 on the pipeline two 102 and the circulating booster pump 13, and a pipeline six valve 1061 is arranged on the pipeline six 106.
The ion exchange system comprises a mixed bed ion exchanger 21 and a front cation bed ion exchanger 22, wherein a mixed bed ion exchanger pipeline I201 and a mixed bed ion exchanger pipeline II 202 are respectively arranged at two ends of the mixed bed ion exchanger 21;
the first mixed bed ion exchanger pipe 201 is connected with a branch pipe 203 and a branch pipe 204,
a branch pipeline III 205, a branch pipeline IV 206 and a condensed water outlet pipeline 401 are connected to the mixed bed ion exchanger pipeline II 202;
the branch pipeline I203 is connected with the condensed water inflow pipeline 301;
the second branch pipe 204 and the fourth branch pipe 206 are converged and connected into the trench 5;
branch line three 205 connects line six 106.
A branch pipeline one valve 2031 is arranged on the branch pipeline one 203;
a branch line two valve 2041 is arranged on the branch line two 204;
a branch pipeline three valve 2051 is arranged on the branch pipeline three 205;
a branch line four valve 2061 is provided in the branch line four 206.
A first preposed cation bed ion exchanger pipeline 221 and a second preposed cation bed ion exchanger pipeline 222 are respectively arranged at two ends of the preposed cation bed ion exchanger 22;
the first preposed cation bed ion exchanger pipe 221 is connected with a fifth branch pipe 223 and a sixth branch pipe 224,
a branch line seven 225, a branch line eight 226 and a branch line nine 227 are connected to the second preposed cation bed ion exchanger line 222;
the branch pipeline five 223 is connected with the condensed water inflow pipeline 301;
branch line six 224 connects branch line four 206;
branch line seven 225 connects line six 106;
branch line eight 226 connects branch line four 206;
the branch pipeline nine 227 is connected with the mixed bed ion exchanger pipeline one 201;
a fifth branch valve 2231 is arranged on the fifth branch 223;
a branch pipeline six valve 2241 is arranged on the branch pipeline six 224;
a branch seven valve 2251 is arranged on the branch seven 225;
a branch pipeline eight valve 2261 is arranged on the branch pipeline eight 226;
a branch pipeline nine valve I2271 and a branch pipeline nine valve II 2272 are arranged on the branch pipeline nine 227;
the condensation water inlet pipeline 301 is characterized by further comprising a pipeline seven 207, wherein one end of the pipeline seven 207 is connected to the junction of the branch pipeline one 203, the branch pipeline five 223 and the condensation water inlet pipeline 301, and the other end of the pipeline seven is connected to the junction of the branch pipeline three 205, the branch pipeline seven 225 and the pipeline six 106; a seventh pipeline valve 2071 is disposed on the seventh pipeline 207.
One end of the condensed water inflow pipeline 301 is provided with a condensed water inlet 31, a condensed water flowmeter 3011 is arranged on the condensed water inflow pipeline 301, and a condensed water inflow pipeline valve 3012;
one end of the condensed water outlet pipeline 401 is a condensed water outlet 41, and a condensed water outlet pipeline valve I4011, a hydrogen conductivity meter 4012, a sodium meter 4013 and a condensed water outlet pipeline valve II 4014 are arranged on the condensed water outlet pipeline 401.
The device is used for carrying out condensate polishing, and comprises the following steps:
(1) and (3) treating condensed water:
condensed water enters the pre-cation bed ion exchanger 22 through a condensed water inlet 31, a condensed water flowmeter 3011, a condensed water inflow pipeline valve 3012 and a branch pipeline five-valve 2231, and then enters the mixed bed ion exchanger 21 through a branch pipeline nine-valve one 2271 and a branch pipeline nine-valve two 2272; fe in the condensed water in the cation bed pre-exchanger 223+And part of Na+Removal by cation exchange, the ion exchange reaction formula: RNH4+Fe3++Na+→RFe+RNa+NH4 +(ii) a In the mixed bed ion exchanger 21, Cl in the condensed water－、SO4 2－And the rest of Na+Removal by anion exchange and cation exchange, the ion exchange reaction formula: ROH + Cl－+SO4 2－→RCl+RSO4+OH－，RNH4+Na+→RNa+NH4 +The condensed water is purified; the purified condensed water is delivered to a steam-water system of a power plant unit through a condensed water outlet pipe valve II 4014, a sodium meter 4013, a hydrogen conductivity meter 4012 and a pipe valve I4011; when the hydrogen conductivity meter 4012 and the sodium degree meter 4013 show that the quality of the treated water of the mixed bed ion exchanger 21 approaches the quality limit index of the treated water of the condensed water, the operation process is finished.
(2) Ion exchange resin backwashing:
starting the circulating booster pump 13, leading the demineralized water in the demineralized water tank 14 to enter the preposed cation bed ion exchanger 22 through a pipeline four-valve 1041, a conductivity meter 1032, an ammonia water flow meter 1033, the circulating booster pump 13 and a pipeline six-valve 1061, and then enter the mixed bed ion exchanger 21 through a branch pipeline seven-valve 2251, and backwashing the cation exchange resin and the mixed ion exchange resin; the backwash effluent is discharged into the trench 5 through a six-way valve 2241 and a two-way valve 2041.
(3) Ion exchange resin regeneration:
preparing ammonia water: according to the quantity of the ion exchange resin to be regenerated and the regeneration requirement, presetting the volume and concentration of the prepared ammonia water, starting a circulating booster pump 13, and adding a preset quantity of demineralized water into an ammonia water tank 11 through a four-valve pipe 1041, a conductivity meter 1032, an ammonia water flow meter 1033, the circulating booster pump 13, a two-valve pipe 1021 and a mixer 12; then, the four valves 1041 of the pipeline are closed, the three valves 1031 of the pipeline are opened, and the demineralized water is circulated among the ammonia water tank 11, the mixer 12 and the circulating booster pump 13; slowly opening a five-valve 1051 of the pipeline, enabling liquid ammonia to enter a mixer 12, mixing and dissolving the liquid ammonia with demineralized water, enabling the liquid ammonia to enter an ammonia water tank 11, and circulating among the ammonia water tank 11, the mixer 12 and a circulating booster pump 13; and reading the conductivity value of the prepared ammonia water through a conductivity meter 1032, closing the five-pipeline valve 1051 when the conductivity value reaches a preset value, continuously running the circulating booster pump 13 for 10 minutes, and then closing the two-pipeline valve 1021, the circulating booster pump 13 and the three-pipeline valve 1031 in sequence to finish the preparation of the ammonia water.
Regeneration: starting the circulating booster pump 13, making the ammonia water enter the mixed bed ion exchanger 21 through the three-valve pipeline 1031, the conductivity meter 1032, the ammonia water flow meter 1033, the circulating booster pump 13, the six-valve pipeline 1061 and the three-valve branch pipeline 2051, and simultaneously regenerating the cation exchange resin and the anion exchange resin in the failed mixed ion exchange resin, wherein the ion exchange reaction formula is as follows: RCl + RSO4+OH－→ROH+Cl－+SO4 2－，RNa+NH4 +→RNH4+Na+(ii) a The regenerated waste liquid discharged from the mixed bed ion exchanger 21 enters the pre-cation bed ion exchanger 22 through a branch pipe nine-valve two 2272 and a branch pipe nine-valve one 2271, and the spent cation exchange resin is regenerated, and the ion exchange reaction formula is as follows: RNA + RFe + NH4 +→RNH4+Na++Fe3+(ii) a The regenerated waste liquid discharged from the cation bed ion exchanger 22 is discharged to the trench 5 through a six-way valve 2241.
And (3) replacement: after the ammonia water is used, opening the four-valve 1041 of the pipeline, closing the three-valve 1031 of the pipeline, and replacing the regeneration waste liquid and the residual ammonia water in the mixed bed ion exchanger 21 and the pre-cation bed ion exchanger 22 by the desalted water according to the way through which the ammonia water flows; after the replacement, the regeneration process is completed.
(4) Washing in a normal way:
the demineralized water in the demineralized water tank 14 enters the pre-cation bed ion exchanger 22 through a four-valve 1041 pipeline, a conductivity meter 1032, an ammonia water flow meter 1033, a circulating booster pump 13, a six-valve 1061 pipeline, a seven-valve 2071 pipeline and a five-valve 2231 branch pipeline, positive ion exchange resin in the pre-cation bed ion exchanger 22 is washed, and positive washing effluent is discharged through an eight-valve 2261 branch pipeline and enters the trench 5. After about 10 minutes of the positive ion exchange resin forward washing process in the preposed cation bed ion exchanger 22, the branch pipeline eight valve 2261 is closed, so that the washing water enters the mixed bed ion exchanger 21 for forward washing of the mixed ion exchange resin through the branch pipeline nine valve I2271 and the branch pipeline nine valve II 2272, the forward washing water is discharged through the branch pipeline four valve 2061 and enters the trench 5, and the forward washing process is finished.
The four steps are circularly reciprocated, and the condensed water fine treatment device of the power plant continuously operates.
Example 3
As shown in fig. 5-6, a power plant condensate polishing apparatus includes an ammonia water preparation system, an ion exchange system, a condensate inflow pipe 301 and a condensate outflow pipe 401;
the ammonia water preparation system comprises an ammonia water tank 11, a mixer 12, a circulating booster pump 13, a desalting water tank 14 and a liquid ammonia tank 15;
the ammonia water tank 11 is connected with the mixer 12 through a first pipeline 101, the mixer 12 is connected with the circulating booster pump 13 through a second pipeline 102, and the circulating booster pump 13 is connected with the ammonia water tank 11 through a third pipeline 103;
the desalted water tank 14 is connected to the third pipeline 103 through the fourth pipeline 104;
the liquid ammonia tank 15 is connected to the mixer 12 through a line five 105.
A second pipeline 102 is provided with a second pipeline valve 1021;
a third pipeline 103 is provided with a third pipeline valve 1031, a conductivity meter 1032 and an ammonia water flow meter 1033;
a pipeline four valve 1041 is arranged on the pipeline four 104;
a fifth pipeline valve 1051 is arranged on the fifth pipeline 105;
a pipeline six 106 is branched from the pipeline two valve 1021 on the pipeline two 102 and the circulating booster pump 13, and a pipeline six valve 1061 is arranged on the pipeline six 106.
The ion exchange system comprises an anion bed ion exchanger 23 and an cation bed ion exchanger 24, wherein a first anion bed ion exchanger pipeline 231 and a second anion bed ion exchanger pipeline 232 are respectively arranged at two ends of the anion bed ion exchanger 23; two ends of the cation bed ion exchanger 24 are respectively provided with a cation bed ion exchanger pipeline I241 and a cation bed ion exchanger pipeline II 242;
the first anion bed ion exchanger pipe 231 is connected with a branch pipe ten 233, a branch pipe eleven 234 and a branch pipe twelve 235,
a branch pipeline thirteen 236, a branch pipeline fourteen 237, a branch pipeline fifteen 238 and a condensed water outlet pipeline 401 are connected to the anion bed ion exchanger pipeline two 232;
the first cation bed ion exchanger line 241 is connected with a branch line sixteen 243 and a branch line seventeen 244,
the cation bed ion exchanger pipe II 242 is connected with a branch pipe eighteen 245 and a branch pipe nineteen 246;
the branch line ten 233 and the connecting branch line sixteen 243 are connected with the condensed water inflow pipeline 301;
branch line eleven 234, branch line seventeen 244, branch line fifteen 238, and branch line nineteen 246 join and connect to trench 5;
a branch pipe twelve 235 is connected with a cation bed ion exchanger pipe two 242;
a branch pipeline thirteen 236 is connected with a cation bed ion exchanger pipeline I241;
the branch line fourteen 237 and the branch line eighteen 245 are connected to the line six 106.
A branch pipeline ten valve 2331 is arranged on the branch pipeline ten 233;
a branch pipeline eleven valve 2341 is arranged on the branch pipeline eleven 234;
a branch pipeline twelve valve first 2351 and a branch pipeline twelve valve second 2352 are arranged on the branch pipeline twelve 235;
a branch pipeline thirteen valve 2361 and a branch pipeline thirteen valve 2362 are arranged on the branch pipeline thirteen 236;
a branch line fourteen valve 2371 is arranged on the branch line fourteen 237;
a fifteen-branch valve 2381 is arranged on the fifteen-branch 238;
a sixteen-branch-pipe valve 2431 is arranged on the sixteen 243 branch pipes;
a branch pipe seventeen valve 2441 is arranged on the branch pipe seventeen 244;
a branch pipeline eighteen valve 2451 is arranged on the branch pipeline eighteen 245;
a branch pipe nineteen valve 2461 is arranged on the branch pipe nineteen 246;
the condensation water inlet pipeline 301 is characterized by further comprising a pipeline seven 207, wherein one end of the pipeline seven 207 is connected to the junction of the branch pipeline ten 233, the branch pipeline sixteen 243 and the condensation water inlet pipeline 301, and the other end of the pipeline seven is connected to the junction of the branch pipeline fourteen 237, the branch pipeline eighteen 245 and the pipeline six 106; a seventh pipeline valve 2071 is disposed on the seventh pipeline 207.
One end of the condensed water inflow pipeline 301 is provided with a condensed water inlet 31, a condensed water flowmeter 3011 is arranged on the condensed water inflow pipeline 301, and a condensed water inflow pipeline valve 3012;
one end of the condensed water outlet pipeline 401 is a condensed water outlet 41, and a condensed water outlet pipeline valve I4011, a hydrogen conductivity meter 4012, a sodium meter 4013 and a condensed water outlet pipeline valve II 4014 are arranged on the condensed water outlet pipeline 401.
Example 4
As shown in fig. 7-8, a power plant condensate polishing apparatus includes an ammonia water preparation system, an ion exchange system, a condensate inflow pipe 301 and a condensate outflow pipe 401;
the ammonia water preparation system comprises an ammonia water tank 11, a mixer 12, a circulating booster pump 13, a desalting water tank 14 and a liquid ammonia tank 15;
the ammonia water tank 11 is connected with the mixer 12 through a first pipeline 101, the mixer 12 is connected with the circulating booster pump 13 through a second pipeline 102, and the circulating booster pump 13 is connected with the ammonia water tank 11 through a third pipeline 103;
the desalted water tank 14 is connected to the third pipeline 103 through the fourth pipeline 104;
the liquid ammonia tank 15 is connected to the mixer 12 through a line five 105.
A second pipeline 102 is provided with a second pipeline valve 1021;
a third pipeline 103 is provided with a third pipeline valve 1031, a conductivity meter 1032 and an ammonia water flow meter 1033;
a pipeline four valve 1041 is arranged on the pipeline four 104;
a fifth pipeline valve 1051 is arranged on the fifth pipeline 105;
a pipeline six 106 is branched from the pipeline two valve 1021 on the pipeline two 102 and the circulating booster pump 13, and a pipeline six valve 1061 is arranged on the pipeline six 106.
The ion exchange system comprises an anion bed ion exchanger 23, an cation bed ion exchanger 24 and a front cation bed ion exchanger 22, wherein a first anion bed ion exchanger pipeline 231 and a second anion bed ion exchanger pipeline 232 are respectively arranged at two ends of the anion bed ion exchanger 23; two ends of the cation bed ion exchanger 24 are respectively provided with a cation bed ion exchanger pipeline I241 and a cation bed ion exchanger pipeline II 242;
the first anion bed ion exchanger pipe 231 is connected with a branch pipe ten 233, a branch pipe eleven 234 and a branch pipe twelve 235,
a branch pipeline thirteen 236, a branch pipeline fourteen 237, a branch pipeline fifteen 238 and a condensed water outlet pipeline 401 are connected to the anion bed ion exchanger pipeline two 232;
the first cation bed ion exchanger line 241 is connected with a branch line sixteen 243 and a branch line seventeen 244,
the cation bed ion exchanger pipe II 242 is connected with a branch pipe eighteen 245 and a branch pipe nineteen 246;
the branch line ten 233 and the connecting branch line sixteen 243 are connected with the condensed water inflow pipeline 301;
branch line eleven 234, branch line seventeen 244, branch line fifteen 238, and branch line nineteen 246 join and connect to trench 5;
a branch pipe twelve 235 is connected with a cation bed ion exchanger pipe two 242;
a branch pipeline thirteen 236 is connected with a cation bed ion exchanger pipeline I241;
the branch line fourteen 237 and the branch line eighteen 245 are connected to the line six 106.
A branch pipeline ten valve 2331 is arranged on the branch pipeline ten 233;
a branch pipeline eleven valve 2341 is arranged on the branch pipeline eleven 234;
a branch pipeline twelve valve first 2351 and a branch pipeline twelve valve second 2352 are arranged on the branch pipeline twelve 235;
a branch pipeline thirteen valve 2361 and a branch pipeline thirteen valve 2362 are arranged on the branch pipeline thirteen 236;
a branch line fourteen valve 2371 is arranged on the branch line fourteen 237;
a fifteen-branch valve 2381 is arranged on the fifteen-branch 238;
a sixteen-branch-pipe valve 2431 is arranged on the sixteen 243 branch pipes;
a branch pipe seventeen valve 2441 is arranged on the branch pipe seventeen 244;
a branch pipeline eighteen valve 2451 is arranged on the branch pipeline eighteen 245;
a branch pipe nineteen valve 2461 is arranged on the branch pipe nineteen 246;
a first preposed cation bed ion exchanger pipeline 221 and a second preposed cation bed ion exchanger pipeline 222 are respectively arranged at two ends of the preposed cation bed ion exchanger 22;
the first preposed cation bed ion exchanger pipe 221 is connected with a fifth branch pipe 223 and a sixth branch pipe 224,
a branch line seven 225, a branch line eight 226, a branch line twenty 228 and a branch line two-229 are connected to the leading cation bed ion exchanger line two 222;
the branch pipeline five 223 is connected with the condensed water inflow pipeline 301;
branch lines six 224 and eight 226 join branch lines eleven 234, seventeen 244, fifteen 238, and nineteen 246 to be connected to trench 5;
branch line seven 225 connects line six 106;
a branch line twenty 228 is connected with a cation bed ion exchanger line I241;
the branch pipeline II I229 is connected with the anion bed ion exchanger pipeline II 232;
a fifth branch valve 2231 is arranged on the fifth branch 223;
a branch pipeline six valve 2241 is arranged on the branch pipeline six 224;
a branch seven valve 2251 is arranged on the branch seven 225;
a branch pipeline eight valve 2261 is arranged on the branch pipeline eight 226;
a branch pipeline twenty-first valve 2281 and a branch pipeline twenty-second valve 2282 are arranged on the branch pipeline twenty 228;
the first branch pipeline 229 is provided with a first branch pipeline valve 2291 and a second branch pipeline valve 2292;
the condensation water inlet pipeline comprises a pipeline seven 207, one end of the pipeline seven 207 is connected to the junction of a branch pipeline five 223, a branch pipeline ten 233 and a branch pipeline sixteen 243 and the condensation water inlet pipeline 301, and the other end of the pipeline seven is connected to the junction of a branch pipeline seven 225, a branch pipeline fourteen 237, a branch pipeline eighteen 245 and a pipeline six 106; a seventh pipeline valve 2071 is disposed on the seventh pipeline 207.
One end of the condensed water inflow pipeline 301 is provided with a condensed water inlet 31, a condensed water flowmeter 3011 is arranged on the condensed water inflow pipeline 301, and a condensed water inflow pipeline valve 3012;
one end of the condensed water outlet pipeline 401 is a condensed water outlet 41, and a condensed water outlet pipeline valve I4011, a hydrogen conductivity meter 4012, a sodium meter 4013 and a condensed water outlet pipeline valve II 4014 are arranged on the condensed water outlet pipeline 401.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. The fine treatment process of the condensed water in the power plant is characterized by comprising the following steps of:
(1) and (3) treating condensed water: refining the condensed water by using ion exchange resin regenerated by ammonia water, wherein Fe in the condensed water3+、Na+、Cl－And SO4 2－Conversion of ions to NH by cation exchange and anion exchange4 +And OH－；
(2) Ion exchange resin backwashing: after the ion exchange resin is invalid, backwashing by using desalted water;
(3) ion exchange resin regeneration: regeneration of spent ion exchange resin, NH in aqueous ammonia using aqueous ammonia4 +Regenerated cation exchange resin, OH－Regenerating the anion exchange resin;
(4) washing in a normal way: the regenerated ion exchange resin was washed with demineralized water.
2. The power plant condensate polishing process of claim 1,
when the mixed bed ion exchanger is adopted as an ion exchange system of the condensate polishing device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters the mixed bed ion exchanger, and cation exchange resin and anion exchange resin in the mixed ion exchange resin are regenerated at the same time;
thirdly, introducing desalted water according to the same flow rate and flow-through way as the ammonia water after the prepared ammonia water is used, and replacing regenerated waste liquid and residual ammonia water in the mixed bed ion exchanger; after the replacement, the regeneration process is completed.
3. The power plant condensate polishing process of claim 1,
when the preposed cation bed ion exchanger and the mixed bed ion exchanger are adopted as the ion exchange system of the condensed water fine treatment device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters the mixed bed ion exchanger, and cation exchange resin and anion exchange resin in the mixed ion exchange resin are regenerated at the same time; then enters a preposed cation bed ion exchanger, and residual NH in the regenerated liquid is discharged by utilizing the mixed bed ion exchanger4 +Regenerating the cation exchange resin;
thirdly, introducing desalted water according to the same flow rate and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the mixed bed ion exchanger and the pre-cation bed ion exchanger; after the replacement, the regeneration process is completed.
4. The power plant condensate polishing process of claim 1,
when the cation bed ion exchanger and the anion bed ion exchanger or the anion bed ion exchanger and the cation bed ion exchanger are adopted as the ion exchange system of the condensed water fine treatment device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters an anion bed ion exchanger and an anion bed ion exchanger in sequence, or enters an anion bed ion exchanger and an cation bed ion exchanger in sequence, cation exchange resin is regenerated in the cation bed ion exchanger, and anion exchange resin is regenerated in the anion bed ion exchanger;
thirdly, introducing desalted water according to the same flow velocity and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the cation bed ion exchanger and the anion bed ion exchanger; after the replacement, the regeneration process is completed.
5. The power plant condensate polishing process of claim 1,
when the preposed cation bed ion exchanger, the cation bed ion exchanger and the anion bed ion exchanger or the preposed cation bed ion exchanger, the anion bed ion exchanger and the cation bed ion exchanger are adopted as the ion exchange system of the condensed water fine treatment device,
the regeneration step of the step (3) is as follows:
firstly, preparing ammonia water according to the quantity of ion exchange resin to be regenerated and the regeneration requirement;
secondly, ammonia water enters an anion bed ion exchanger and an anion bed ion exchanger in sequence, or enters an anion bed ion exchanger and an cation bed ion exchanger in sequence, cation exchange resin is regenerated in the cation bed ion exchanger, and anion exchange resin is regenerated in the anion bed ion exchanger; finally, the cation exchange resin enters a preposed cation bed ion exchanger to regenerate cation exchange resin;
thirdly, introducing desalted water according to the same flow rate and flow path as the ammonia water after the prepared ammonia water is used, and replacing the regenerated waste liquid and residual ammonia water in the cation bed ion exchanger, the anion bed ion exchanger and the preposed cation bed ion exchanger; after the replacement, the regeneration process is completed.
6. The power plant condensate polishing process according to any one of claims 2 to 5,
the flow direction of the ammonia water in the step (3) through the ion exchanger is the same as or opposite to the flow direction of the condensed water in the step (1) through the ion exchanger.
7. A power plant condensed water fine treatment device, which is characterized in that,
comprises an ammonia water preparation system, an ion exchange system, a condensed water inflow pipeline and a condensed water outflow pipeline;
the ammonia water preparation system comprises an ammonia water tank, a mixer, a circulating booster pump, a desalting water tank and a liquid ammonia tank;
the ammonia water tank, the mixer and the circulating booster pump are mutually connected through pipelines to form a circulating loop;
the desalting water tank is connected to a pipeline between the ammonia water tank and the circulating booster pump through a pipeline;
the liquid ammonia tank is connected with the mixer through a pipeline;
the ion exchange system is connected to a pipeline between the mixer and the circulating booster pump through a pipeline;
the condensed water inflow pipeline and the condensed water outflow pipeline are respectively connected with an ion exchange system.
8. The power plant condensate polishing apparatus as claimed in claim 7,
the ion exchange system comprises one or more groups of ion exchangers,
each group of ion exchangers is any one of the following:
firstly, a mixed bed ion exchanger;
② a front cation bed ion exchanger and a mixed bed ion exchanger;
③ cation bed ion exchanger and anion bed ion exchanger;
fourthly, a front cation bed ion exchanger, a cation bed ion exchanger and an anion bed ion exchanger are arranged;
(v) anion bed ion exchanger + cation bed ion exchanger;
sixthly, the preposed cation bed ion exchanger, the anion bed ion exchanger and the cation bed ion exchanger.
9. The power plant condensate polishing apparatus as claimed in claim 7,
a condensed water flow meter is arranged on the condensed water inflow pipeline;
and a hydrogen conductivity meter and a sodium meter are arranged on the condensed water outlet pipeline.
10. The power plant condensate polishing apparatus as claimed in claim 7,
and a conductivity meter and an ammonia water flowmeter are arranged on a pipeline between the ammonia water tank and the circulating booster pump.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114798002A (en) * | 2022-04-15 | 2022-07-29 | 华电电力科学研究院有限公司 | Water-saving recovery method for condensate fine treatment system of thermal power plant |
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