KR20020031858A - Neutralizing method for regeneration waste of ion exchange resin - Google Patents

Neutralizing method for regeneration waste of ion exchange resin Download PDF

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KR20020031858A
KR20020031858A KR1020000062615A KR20000062615A KR20020031858A KR 20020031858 A KR20020031858 A KR 20020031858A KR 1020000062615 A KR1020000062615 A KR 1020000062615A KR 20000062615 A KR20000062615 A KR 20000062615A KR 20020031858 A KR20020031858 A KR 20020031858A
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South Korea
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regeneration waste
exchange resin
carbon dioxide
waste liquid
ion exchange
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KR1020000062615A
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Korean (ko)
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강신경
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신현준
재단법인 포항산업과학연구원
이구택
주식회사 포스코
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Priority to KR1020000062615A priority Critical patent/KR20020031858A/en
Publication of KR20020031858A publication Critical patent/KR20020031858A/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/26—Selective adsorption, e.g. chromatography characterised by the separation mechanism
    • B01D15/36—Selective adsorption, e.g. chromatography characterised by the separation mechanism involving ionic interaction
    • B01D15/361—Ion-exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/20—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the conditioning of the sorbent material
    • B01D15/203—Equilibration or regeneration
    • 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
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment

Abstract

PURPOSE: A method for neutralizing regeneration waste of ion exchange resin in pure water manufacturing system is provided, in which carbon dioxide gas from a carbon dioxide stripping tower is used to neutralize a mixed regeneration waste solution of alkali and acid. CONSTITUTION: Waste acid solution generated from cation exchange resin tower(12) and waste alkali solution generated from anion exchange resin tower(16) flow into a mixed regeneration waste solution tank(21). At this stage, flue gas containing carbon dioxide gas exits a carbon dioxide stripping tower(14) through an exit valve(23) to the outside of system. As the mixed regeneration waste solution, however, exceeds pH 8.6, discharge of the mixed regeneration waste solution outside the tank is restricted because it goes beyond the maximum permissible guideline listed in environmental regulations. In such cases, flue gas containing carbon dioxide gas is supplied into the mixed regeneration waste solution tank by closing the exit valve(23) while opening a connection valve(22). Such operations cause excess alkali contained in regeneration waste solution to react with carbon dioxide gas for neutralization and it is represented by follow chemical equations: (i) CO2 + H2O ↔ H2CO3 ↔ H¬+ + HCO3, (ii) NaOH + H¬+ + HCO3 ↔ NaHCO3 + H2O.

Description

이온교환수지 재생폐액의 중화방법{NEUTRALIZING METHOD FOR REGENERATION WASTE OF ION EXCHANGE RESIN}NEUTRALIZING METHOD FOR REGENERATION WASTE OF ION EXCHANGE RESIN}

본 발명은 재생폐액을 처리하는 방법에 관한 것이며, 특히, 이온교환수지를 이용하는 순수제조 시스템에서 재생공정 중 발생하는 산 및 알칼리 혼합 재생폐액을 공정 중에 탈기탑에서 배출되는 배가스를 이용하여 중화시키는 방법에 관한 것이다.The present invention relates to a method for treating regenerated waste liquid, and in particular, a method for neutralizing acid and alkali mixed regenerated waste liquid generated during a regeneration process in a pure water production system using an ion exchange resin by using exhaust gas discharged from a deaeration tower during the process. It is about.

일반적인 순수제조 공정은 도 1에 도시된 바와 같이 양이온교환탑(12), 탈기탑(14), 음이온교환탑(16)으로 구성되어 있는 이온교환수지 시스템을 이용한다.A general pure water production process uses an ion exchange resin system composed of a cation exchange column 12, a degassing column 14, an anion exchange column 16 as shown in FIG.

상기 양이온교환탑(12) 내에는 양이온교환수지가 충전되어 있는데, 양이온교환수지의 H+이온과 물속의 양이온이 서로 교환되어 제거된다. 이 때, 양이온과 결합하고 있던 HCO3 _이온은 양이온교환수지의 H+이온과 반응하여 물(H2O)과 이산화탄소(CO2)로 된다. 그리고, 음이온교환탑(16) 내에는 음이온교환수지가 충전되어 있어 물속의 음이온을 제거하여 순수를 생산하게 된다.The cation exchange tower 12 is filled with a cation exchange resin, and the H + ions of the cation exchange resin and the cations in the water are exchanged and removed. At this time, HCO 3 _ ions bound to the cation react with H + ions of the cation exchange resin to form water (H 2 O) and carbon dioxide (CO 2 ). And, in the anion exchange tower 16 is filled with anion exchange resin to remove the anions in the water to produce pure water.

이런 순수제조 공정을 간략하면 살펴보면, 정수조(도시안됨)에 모여진 정수를 양이온펌프(11)를 사용하여 양이온교환탑(12)에 공급한다. 그러면, 양이온교환탑(12) 내에 충전된 양이온교환수지에 의해 원수 중에 함유되어 있는 양이온이 앞서 설명한 반응에 의해 제거되고(이런 상태를 '산성연수'라 한다), 이를 탈기탑(14)에 공급하면 그 탈기탑(14)에서는 블로어(13)를 이용하여 산성연수에 함유된 CO2를 대기로 방출한다. 그런 다음, 음이온펌프(15)를 이용하여 이런 상태의 산성연수를 음이온교환탑(16)으로 공급하여 그 내부에 충진된 음이온교환수지를 통해 산성연수 중에 함유된 음이온을 제거함으로써 순수를 생산하게 된다.Briefly looking at such a pure water manufacturing process, purified water collected in a water purification tank (not shown) is supplied to the cation exchange tower 12 using a cation pump (11). Then, the cation contained in the raw water by the cation exchange resin packed in the cation exchange tower 12 is removed by the reaction described above (this state is called 'acid soft water'), and is supplied to the degassing column 14 In the degassing column 14, the blower 13 is used to discharge CO 2 contained in the acidic soft water into the atmosphere. Then, using the anion pump 15 to supply the acidic soft water in this state to the anion exchange tower 16 to remove the anions contained in the acidic soft water through the anion exchange resin filled therein to produce pure water. .

그러나, 이온교환수지는 일정시간(12 ∼ 48시간) 이상 사용하게 되면, 이온교환능력을 상실하게 되어 더 이상 순수를 생산할 수 없게 된다. 이 때에는 이온교환수지를 원래대로 회복시켜 주어야 하는데, 이를 재생(Regeneration)이라고 한다. 이온교환수지의 재생은 주로 약품을 이용하여 재생을 하는데, 양이온교환수지는 펌프(19)에 의해 공급되는 산저장조(17)에 저장된 염산(HCl)이나 황산(H2SO4) 등의 산을 이용하고, 음이온교환수지는 다른 펌프(20)에 의해 공급되는 알칼리저장조(18)에 저장된 가성소다(NaOH) 등의 알칼리를 이용하여 재생하게 된다.However, when the ion exchange resin is used for a predetermined time (12 to 48 hours) or more, the ion exchange capacity is lost and pure water can no longer be produced. At this time, the ion exchange resin should be restored to its original state, which is called regeneration. Regeneration of the ion exchange resin is mainly performed by using chemicals, and the cation exchange resin is used to recover acids such as hydrochloric acid (HCl) or sulfuric acid (H 2 SO 4 ) stored in the acid storage tank 17 supplied by the pump 19. In this case, the anion exchange resin is regenerated using alkali such as caustic soda (NaOH) stored in an alkali storage tank 18 supplied by another pump 20.

그러나, 이온교환탑(12, 14)내에서의 이온교환수지의 재생효율은 낮기 때문에, 이론량의 200∼500% 정도의 재생제가 필요하게 된다. 따라서, 재생시에는 양이온교환탑(12)에서는 산 폐액이, 음이온교환탑(14)에서는 알칼리 폐액이 각각 발생하게 되며, 이들 폐액은 재생폐액 집수조(21)에 모이게 된다. 그러나, 산 폐액과 알칼리 폐액의 당량이 서로 일치하지 않을 경우에는 혼합 재생폐액의 수소이온농도가 배출기준 5.8 ∼ 8.6의 범위를 벗어나는 경우가 있다. 이 때에는 혼합 재생폐액을 별도의 산이나 알칼리로 다시 중화하여 배출기준 이내로 처리한 후에 배출해야 하기 때문에, 별도의 재생폐액의 처리비용이 소요되는 단점이 있다.However, since the regeneration efficiency of the ion exchange resin in the ion exchange towers 12 and 14 is low, a regenerant of about 200 to 500% of the theoretical amount is required. Therefore, during the regeneration, an acid waste liquid is generated in the cation exchange tower 12 and an alkaline waste liquid is generated in the anion exchange tower 14, and these waste liquids are collected in the regeneration waste liquid collection tank 21. However, when the equivalents of the acid waste liquid and the alkaline waste liquid do not coincide with each other, the hydrogen ion concentration of the mixed regeneration waste liquid may be out of the range of emission standards 5.8 to 8.6. In this case, since the mixed regeneration waste liquid is neutralized again with a separate acid or alkali and must be discharged after being treated within an emission standard, there is a disadvantage in that a separate regeneration waste liquid treatment cost is required.

앞서 설명한 이온교환수지 재생방법에 관한 종래기술로는 "순수제조용 수지 재생시스템(대한민국 특허공개 제1998-048454호)", "이온교환탑의 재생방법 및 장치(대한민국 특허공개 제1997-014837호)" 등이 있지만, 이들 기술은 이온교환수지 재생방법에 관한 것으로서, 혼합 재생폐액의 처리는 별도의 산이나 알칼리를 이용하는 방법을 채택하고 있다.Prior arts related to the ion exchange resin regeneration method described above include "Resin recycling system for pure water production (Korean Patent Publication No. 1998-048454)", "Regeneration method and apparatus for ion exchange tower (Korean Patent Publication No. 1997-014837) Although these techniques are related to the ion exchange resin regeneration method, the mixed regeneration waste liquid is treated with a separate acid or alkali.

따라서, 본 발명은 앞서 설명한 바와 같은 종래기술의 문제점을 해결하기 위하여 안출된 것으로서, 이온교환수지 시스템에서 발생하는 혼합 재생폐액을 배출기준 이내로 처리하기 위하여 공정 중에 탈기탑에서 배출되는 배가스를 이용함으로써, 재생폐액의 처리비용을 최소화할 수 있는 이온교환수지 재생폐액의 중화방법을 제공하는 데 그 목적이 있다.Accordingly, the present invention has been made to solve the problems of the prior art as described above, by using the exhaust gas discharged from the degassing column during the process to treat the mixed regeneration waste liquid generated in the ion exchange resin system within the emission standard, An object of the present invention is to provide a method for neutralizing an ion exchange resin regeneration waste liquid, which can minimize the treatment cost of regeneration waste liquid.

도 1은 종래기술에 따른 이온교환수지 시스템의 개략도이고,1 is a schematic diagram of an ion exchange resin system according to the prior art,

도 2는 본 발명의 한 실시예에 따른 이온교환수지 재생폐액의 중화방법을 설명하기 위한 이온교환수지 시스템의 개략도이다.Figure 2 is a schematic diagram of an ion exchange resin system for explaining the neutralization method of the ion exchange resin regeneration waste liquid according to an embodiment of the present invention.

♠ 도면의 주요부분에 대한 부호의 설명 ♠♠ Explanation of symbols on the main parts of the drawing ♠

11 : 양이온펌프 12 : 양이온교환탑11: cation pump 12: cation exchange tower

13 : 블로어 14 : 탈기탑13: blower 14: degassing tower

15 : 음이온펌프 16 : 음이온교환탑15 anion pump 16 anion exchange tower

17 : 산저장조 18 : 알칼리저장조17 acid storage tank 18 alkali storage tank

19, 20 : 펌프 21 : 재생폐액 집수조19, 20: pump 21: recycling waste collection tank

22 : 연결밸브 23 : 배출밸브22: connection valve 23: discharge valve

위와 같은 목적을 달성하기 위한 본 발명에 따르면, 양이온교환탑과 탈기탑 및 음이온교환탑을 포함하는 이온교환수지 시스템의 상기 양이온교환탑 및 음이온교환탑에서 각각 생성되는 산 폐액 및 알칼리 폐액이 혼합되어 생성된 이온교환수지 재생폐액을 중화하는 방법에 있어서, 상기 이온교환수지 재생폐액에 상기 탈기탑에서 배출되는 이산화탄소(CO2)를 함유한 배가스를 혼입하여 상기 재생폐액을 중화 처리하는 이온교환수지 재생폐액의 중화방법이 제공된다.According to the present invention for achieving the above object, the acid and liquid wastes generated in the cation exchange tower and the anion exchange column of the ion exchange resin system including a cation exchange tower and a degassing column and an anion exchange tower are mixed A method of neutralizing the generated ion exchange resin regeneration waste liquid, wherein the ion exchange resin regeneration waste liquid is mixed with exhaust gas containing carbon dioxide (CO 2 ) discharged from the degassing tower to neutralize the regeneration waste liquid. A method of neutralizing waste fluid is provided.

또한, 본 발명에 따르면, 상기 이산화탄소를 함유한 배가스는 상기 재생폐액에서 알칼리 성분을 중화처리한다.Further, according to the present invention, the exhaust gas containing carbon dioxide neutralizes the alkaline component in the regeneration waste liquid.

아래에서, 본 발명에 따른 이온교환수지 재생폐액의 중화방법의 양호한 실시예를 첨부한 도면을 참조로 하여 상세히 설명하겠다.Hereinafter, with reference to the accompanying drawings a preferred embodiment of the neutralization method of the ion exchange resin regeneration waste liquid according to the present invention will be described in detail.

도면에서, 도 2는 본 발명의 한 실시예에 따른 이온교환수지 재생폐액의 중화방법을 설명하기 위한 이온교환수지 시스템의 개략도이다.2 is a schematic diagram of an ion exchange resin system for explaining a method for neutralizing an ion exchange resin regeneration waste liquid according to an embodiment of the present invention.

도 2에 보이듯이, 본 발명에 사용되는 이온교환수지 시스템은 공정 중에 탈기탑(14)에서 배출되는 이산화탄소(CO2)를 함유한 배가스를 필요에 따라 선택적으로 이용할 수 있도록, 탈기탑(14)과 재싱폐액 집수조(21)를 서로 연결하는 연결밸브(22)와 외부로 직접배출하는 배출밸브(23)를 구비한 것을 제외하고는 도 1에 도시된 이온교환 시스템과 동일한 구성요소들로 구성되어 있다. 그러므로, 동일한 구성요소에 대해서는 동일한 도면번호가 부여될 것이며, 이것들에 관한 설명은 여기에서 생략하기로 한다.As shown in FIG. 2, the ion exchange resin system used in the present invention may use the exhaust gas containing carbon dioxide (CO 2 ) discharged from the degassing tower 14 during the process to selectively use as needed. It is composed of the same components as the ion exchange system shown in FIG. 1 except that it has a connection valve 22 for connecting the first and second wastewater collection tank 21 and a discharge valve 23 for direct discharge to the outside. have. Therefore, the same reference numerals will be given to the same components, and description thereof will be omitted here.

도 2에 보이듯이, 본 발명은 이온교환수지 시스템에서 발생하는 재생폐액을 공정 중에 탈기탑(14)에서 배출되는 이산화탄소를 함유한 배가스를 선택적으로 이용하여 중화시킴으로써, 재생폐액과 배가스를 모두 효과적으로 처리하는 것이다.As shown in FIG. 2, the present invention effectively neutralizes the regeneration waste liquid generated in the ion exchange resin system by selectively using a flue gas containing carbon dioxide discharged from the degassing column 14 during the process, thereby effectively treating both the regeneration waste liquid and the exhaust gas. It is.

본 발명에서 산 폐액은 양이온교환탑(12)에서, 알칼리 폐액은 음이온교환탑(16)에서 각각 발생되어 재생폐액 집수조(21)에 유입되어 혼합된다. 이 때, 공정 중에 탈기탑(14)에서 배출되는 이산화탄소를 함유한 배가스는 배출밸브(23)를 통해 외부로 배출된다.In the present invention, the acid waste liquid is generated in the cation exchange tower 12 and the alkaline waste liquid is respectively generated in the anion exchange tower 16 and flows into the regeneration waste collection tank 21 to be mixed. At this time, the exhaust gas containing carbon dioxide discharged from the degassing column 14 during the process is discharged to the outside through the discharge valve (23).

그러다가, 유입 혼합된 재생폐액의 수소이온농도가 8.6을 초과하는 알칼리성일 경우에는, 배출허용기준 범위를 벗어나게 되어 집수조(21)에 저장된 재생폐액을 외부로 배출할 수 없게 된다. 이 때에는 배출밸브(23)를 닫고 연결밸브(22)를 열어 공정 중 탈기탑(14)에서 배출되는 이산화탄소를 함유한 배가스를 재생폐액 집수조(21)에 공급한다. 그러면, 이산화탄소가 재생폐액 중 알칼리 성분과 반응하여 중성이 되어, 수소이온농도가 배출허용기준 범위를 만족하면 재생폐액을 외부로 배출하게 된다.Then, when the hydrogen ion concentration of the inflow-mixed regeneration waste liquid is more than 8.6, it is out of the discharge allowance standard range and the regeneration waste liquid stored in the sump tank 21 cannot be discharged to the outside. In this case, the discharge valve 23 is closed and the connection valve 22 is opened to supply the exhaust gas containing carbon dioxide discharged from the degassing tower 14 during the process to the regeneration waste collection tank 21. Then, the carbon dioxide reacts with the alkali component in the regeneration waste solution and becomes neutral, and when the hydrogen ion concentration satisfies the emission allowance standard range, the regeneration waste liquid is discharged to the outside.

재생폐액 집수조(21) 내에서 알칼리 폐액과 배가스 중의 이산화탄소의 중화반응은 반응식 1, 반응식 2와 같이 반응하여, 알칼리성 폐액이 중성으로 변한다.The neutralization reaction of the alkaline waste liquid and the carbon dioxide in the flue gas in the regeneration waste liquid collecting tank 21 reacts as shown in Schemes 1 and 2, and the alkaline waste liquid is changed to neutral.

CO2+ H2O ↔ H2CO3↔ H++ HCO3 _ CO 2 + H 2 O ↔ H 2 CO 3 ↔ H + + HCO 3 _

NaOH + H++ HCO3 _↔ NaHCO3+ H2ONaOH + H + + HCO 3 _ ↔ NaHCO 3 + H 2 O

<실험예>Experimental Example

이 실험예는 알칼리성의 재생폐액을 공정 중의 탈기탑(14)에서 발생하는 이산화탄소를 함유한 배가스를 이용하여 중화시키는 경우 그 효과를 알아보기 위한 것이다.This experimental example is to find the effect of the alkaline regeneration waste liquid when the neutralization using the exhaust gas containing the carbon dioxide generated in the degassing column 14 during the process.

이를 위해 처리용량이 0.5㎥/hr인 순수제조 파일럿 테스트(Pilot test)장치를 도 1에 도시된 이온교환수지 시스템과 같이 구성하여 24시간 운전 후 표 1과 같은 조건으로 재생을 실시하였다.To this end, a pilot production test device having a processing capacity of 0.5 m 3 / hr was configured as the ion exchange resin system shown in FIG. 1 and regenerated under the conditions shown in Table 1 after 24 hours of operation.

구분division 양이온교환탑Cation exchange tower 음이온교환탑Anion exchange tower 수지충전부피(L)Resin filling volume (L) 1818 2424 재생약품Regenerator HClHCl NaOHNaOH 재생레벨(g/L)Regeneration level (g / L) 5050 4040

표 1과 같은 조건에서 재생을 실시하여 양이온교환탑(12)의 산 폐액과 음이온교환탑(16)의 알칼리 폐액을 재생폐액 집수조(21) 내에 혼합한 결과, 재생폐액의 양은 126L 이었고, 수소이온농도는 9.2 이었다. 이 후, 원수를 0.5㎥/hr 의 유량으로 파일럿 플랜트[Pilot plant, 양이온교환탑(12), 탈기탑(14) 및 음이온교환탑(16)]로 유입하면서 통수를 실시하였고, 탈기탑(14)의 블로어(13)는 50L/min 의 유량으로 가동하였으며, 이 때 배가스 중의 이산화탄소의 함량은 0.2%(공기 중 이산화탄소의 함량 : 0.03%)이었다. 이 때, 재생폐액 집수조(21)와 연통하는 연결밸브(22)를 열어 배가스를 혼합 재생폐액이 들어 있는 재생폐액 집수조(21)에 주입하기 시작하니, 1시간 후에는 수소이온농도가 8.5, 4시간 이후에는 7.0 으로 중화되는 것을 관찰할 수 있었다.Regeneration was carried out under the conditions as shown in Table 1, and the acid waste liquid of the cation exchange tower 12 and the alkaline waste liquid of the anion exchange tower 16 were mixed in the regeneration waste liquid collection tank 21. As a result, the amount of the regeneration waste liquid was 126 L. The concentration was 9.2. Thereafter, the raw water was flowed into the pilot plant [Pilot plant, cation exchange tower 12, degassing tower 14 and anion exchange tower 16] at a flow rate of 0.5 m 3 / hr, and degassing tower 14 Blower 13) was operated at a flow rate of 50L / min, the carbon dioxide content in the exhaust gas was 0.2% (content of carbon dioxide in the air: 0.03%). At this time, the connection valve 22 communicating with the regeneration waste collection tank 21 is opened, and the flue gas is started to be injected into the regeneration waste collection tank 21 containing the mixed regeneration waste liquid. After time it was observed to neutralize to 7.0.

상기와 같은 방법으로 운전된 혼합 재생폐액의 시간에 따른 수소이온농도를 측정한 결과가 표 2에 나타나 있다.Table 2 shows the result of measuring the hydrogen ion concentration with time of the mixed regeneration waste liquid operated in the above manner.

운전시간(hr)Operating hours (hr) 수소이온농도Hydrogen ion concentration 00 9.29.2 1One 8.58.5 22 8.08.0 44 7.07.0 88 6.86.8 1212 6.66.6 2424 6.56.5

표 2에서 알 수 있는 바와 같이, 탈기탑(14)에서 발생하는 배가스를 이용하여 재생폐액을 중화 처리함으로써, 수소이온농도를 배출허용기준 범위 내로 처리할 수 있음을 확인할 수 있었으며, 다른 별도의 산을 이용하는 방법보다 경제적임을 알 수 있었다.As can be seen in Table 2, by neutralizing the regeneration waste liquid using the exhaust gas generated in the degassing column 14, it was confirmed that the hydrogen ion concentration can be treated within the emission allowance standard range, another separate acid It was found to be more economic than using the method.

앞서 상세히 설명한 바와 같이 본 발명의 이온교환수지 재생폐액의 중화방법은 이용교환수지를 이용한 순수제조 시스템에서 발생하는 알칼리성의 혼합 재생폐액을 탈기탑에서 배출되는 이산화탄소를 함유한 배가스를 이용하여 중화시킴으로써, 수소이온농도를 배출허용기준 이내로 처리할 수 있음은 물론 재생폐액을 중화시키기 위해 별도로 주입되는 산을 사용하지 않음으로 인하여 경제적인 효과가 있다.As described in detail above, the neutralization method of the ion exchange resin regeneration waste liquid of the present invention is neutralized by using the flue gas containing carbon dioxide discharged from the degassing column of the alkaline mixed regeneration waste liquid generated in the pure water production system using the use exchange resin, Hydrogen ion concentration can be treated within the emission limit, and there is an economic effect because it does not use an acid injected separately to neutralize the regeneration waste liquid.

이상에서 본 발명의 이온교환수지 재생폐액의 중화방법에 대한 기술사항을 첨부도면과 함께 서술하였지만 이는 본 발명의 가장 양호한 실시예를 예시적으로 설명한 것이지 본 발명을 한정하는 것은 아니다.Although the technical details of the method for neutralizing the ion exchange resin regeneration waste liquid of the present invention have been described together with the accompanying drawings, this is illustrative of the best embodiments of the present invention and is not intended to limit the present invention.

또한, 이 기술분야의 통상의 지식을 가진 자이면 누구나 본 발명의 기술사상의 범주를 이탈하지 않는 범위내에서 다양한 변형 및 모방이 가능함은 명백한 사실이다.In addition, it is obvious that any person skilled in the art can make various modifications and imitations without departing from the scope of the technical idea of the present invention.

Claims (2)

양이온교환탑과 탈기탑 및 음이온교환탑을 포함하는 이온교환수지 시스템의 상기 양이온교환탑 및 음이온교환탑에서 각각 생성되는 산 폐액 및 알칼리 폐액이 혼합되어 생성된 이온교환수지 재생폐액을 중화하는 방법에 있어서,In the method for neutralizing the ion exchange resin regeneration waste liquid generated by mixing the acid waste liquid and the alkaline waste liquid generated in the cation exchange tower and the anion exchange column of the ion exchange resin system including a cation exchange column, a degassing column and an anion exchange column In 상기 이온교환수지 재생폐액에 상기 탈기탑에서 배출되는 이산화탄소(CO2)를 함유한 배가스를 혼입하여 상기 재생폐액을 중화 처리하는 것을 특징으로 이온교환수지 재생폐액의 중화방법.And neutralizing the regeneration waste liquid by mixing exhaust gas containing carbon dioxide (CO 2 ) discharged from the deaeration tower into the regeneration waste liquid of the ion exchange resin. 제1항에 있어서, 상기 이산화탄소를 함유한 배가스는 상기 재생폐액에서 알칼리 성분을 중화처리하는 것을 특징으로 하는 이온교환수지 재생폐액의 중화방법.The method of claim 1, wherein the exhaust gas containing carbon dioxide neutralizes an alkaline component in the regeneration waste liquid.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100473519B1 (en) * 2002-07-25 2005-03-10 한국에너지기술연구원 Multiple steps type of alkali waste water neutralization system and its neutralization method
KR100892257B1 (en) * 2007-08-20 2009-04-09 (주)우리텍 A Process Steam Condensate Recycling Apparatus
KR101280357B1 (en) * 2013-03-14 2013-07-01 (주) 시온텍 Ion-exchange water softening system and process re-using concentrate and brine waste

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US4448693A (en) * 1981-01-28 1984-05-15 Kernforschungszentrum Karlsruhe Gmbh Method for partially desalinating water with a weakly acid and strongly basic ion exchanger materials and subsequently regenerating the ion exchanger materials
KR19980048454A (en) * 1996-12-17 1998-09-15 김종진 Pure Resin Regeneration System
KR0156605B1 (en) * 1995-09-27 1998-12-15 이규철 Regeneration method and appartus of ion exchange tower

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4448693A (en) * 1981-01-28 1984-05-15 Kernforschungszentrum Karlsruhe Gmbh Method for partially desalinating water with a weakly acid and strongly basic ion exchanger materials and subsequently regenerating the ion exchanger materials
KR0156605B1 (en) * 1995-09-27 1998-12-15 이규철 Regeneration method and appartus of ion exchange tower
KR19980048454A (en) * 1996-12-17 1998-09-15 김종진 Pure Resin Regeneration System

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100473519B1 (en) * 2002-07-25 2005-03-10 한국에너지기술연구원 Multiple steps type of alkali waste water neutralization system and its neutralization method
KR100892257B1 (en) * 2007-08-20 2009-04-09 (주)우리텍 A Process Steam Condensate Recycling Apparatus
KR101280357B1 (en) * 2013-03-14 2013-07-01 (주) 시온텍 Ion-exchange water softening system and process re-using concentrate and brine waste

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