JP3555997B2 - Purification method of acrylamide aqueous solution - Google Patents
Purification method of acrylamide aqueous solution Download PDFInfo
- Publication number
- JP3555997B2 JP3555997B2 JP28040694A JP28040694A JP3555997B2 JP 3555997 B2 JP3555997 B2 JP 3555997B2 JP 28040694 A JP28040694 A JP 28040694A JP 28040694 A JP28040694 A JP 28040694A JP 3555997 B2 JP3555997 B2 JP 3555997B2
- Authority
- JP
- Japan
- Prior art keywords
- acrylamide
- copper
- exchange resin
- ion exchange
- type
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【０００１】
【産業上の利用分野】
本発明はアクリロニトリルの接触水和法により得られるアクリルアミド水溶液を精製する際の脱銅方法に関するものである。
【０００２】
【従来の技術】
アクリルアミドは紙力増強剤、凝集剤などに利用されるアクリルアミド系ポリマーの製造に用いられるほか多方面の用途に向けられる産業上有用なモノマーである。
金属銅系触媒の存在下にアクリロニトリルを接触水和してアクリルアミドを製造する方法はすでに良く知られている。しかして、この銅系触媒を使用して得られたアクリルアミド含有反応液中には微量の銅が溶出して来るのを避けることができない。そのため、アクリルアミド水溶液を原料としてポリマーを製造しようとする場合、そこに溶存する銅は重合反応を阻害するので、アクリルアミド水溶液の商品価値を著しく低下させる原因となる。従って該アクリルアミド反応液から得られるアクリルアミド水溶液をポリマー原料として使用するためには溶存銅を除去する必要がある。溶存銅の除去方法としては強酸性陽イオン交換樹脂により処理する方法やイミノジ酢酸型の弱酸性イオン交換樹脂により処理する方法がとられている。
【０００３】
【発明が解決しようとする課題】
しかしながらアクリルアミドは反応性に富むため、アクリルアミドを重合させることなく工業的にアクリルアミド水溶液中に溶存する銅を除去することはきわめて難しい。たとえば強酸性イオン交換樹脂を使用する場合、遊離酸型（Ｈ型と略称する）であれば銅除去能力は大きいものの、官能基が強酸性であるため、反応性の高いアクリルアミドが重合することは避けられない。これがナトリウム塩型（Ｎａ型と略称する）である場合、アクリルアミドの重合は避けられるものの、銅の吸着能力が劣り十分な除去性能が得られない。またイミノジ酢酸型の弱酸性イオン交換樹脂を使用した場合、それらがＨ型であると弱酸性のために解離が弱く銅の吸着能が弱い。またさらにＮａ型であると官能基が弱酸性であるために、逆にアクリルアミド水溶液にＮａイオンが溶出するという不都合が生じる。
【０００４】
【課題を解決するための手段】
すなわち、本発明は、アクリロニトリルの接触水和法により得られるアクリルアミド水溶液を、アミノリン酸型中酸性イオン交換樹脂により処理することを特徴とするアクリルアミド水溶液の精製方法に関するものである。
本発明はアクリロニトリルの接触水和法により得られるアクリルアミド水溶液から銅を除去するする際、アミノリン酸型の中酸性イオン交換樹脂にて脱銅する方法を提供するものであるが、このようなアミノリン酸型中酸性イオン交換樹脂を使用すると、その強い銅吸着能力により極低濃度にまで銅を除去することが可能であるばかりでなく、中酸性であるために、反応性の高いアクリルアミドにおいてもその重合や加水分解が起こらず、さらにはイオン交換樹脂からＮａイオンなどの溶出もないという非常に高度なアクリルアミド精製が実施できるのである。
【０００５】
以下、本発明を詳細に説明する。
本発明に用いられるアクリルアミド水溶液は、アクリロニトリルを原料として通常の接触水和法により得られる。すなわちアクリロニトリルを水とともに耐圧の反応器に仕込み金属銅触媒の存在下、７０〜１５０℃程度の温度で１〜３時間程度反応させる。得られた反応液には未反応のアクリロニトリルが残存するので、通常これを予め除去しておく。
【０００６】
本発明で処理するアクリルアミド水溶液のアクリルアミド濃度に制限はないが、通常接触水和法により得られるアクリルアミド水溶液中のアクリルアミド濃度は２０〜６０％程度であり、この範囲のアクリルアミド水溶液を好適に処理することができる。もちろん、この範囲外のものであっても適用可能である。
【０００７】
本発明で処理するアクリルアミド水溶液中の銅濃度に制限はないが、接触水和法では通常反応液中に１０〜２００ｐｐｍ程度の銅を含有しており、このようなアクリルアミド水溶液を好適に処理することができる。もちろん、これより大なる濃度もしくは少ない濃度の銅濃度のものであっても、本発明が好適に適用できるものであることは容易に理解できるであろう。
【０００８】
本発明で使用する中酸性イオン交換樹脂とは、スチレン−ジビニルベンゼン共重合体を母体とするアミノリン酸型の中酸性イオン交換樹脂であり、この種の中酸性イオン交換樹脂としては、例えばレバチットＯＣ１０６０（バイエル社製）、デュオライトＣ４６７（ロームアンドハース社製）等の名称で市販されており、好適に使用できる。
【０００９】
本発明で使用する該中酸性イオン交換樹脂はＨ型であってもＮａ型としてもよい。Ｎａ型として使用する場合、その調整方法は該樹脂のイオン交換容量より過剰当量の苛性ソーダ水溶液を接触させればよい。また銅吸着後の該樹脂は鉱酸で処理すればＨ型として使用でき、さらに苛性ソーダ水溶液で同様の処理をすればＮａ型とし再度使用に供することができる。
【００１０】
本発明におけるアクリルアミド水溶液をアミノリン酸型中酸性イオン交換樹脂により処理するとは、要するに該水溶液を該イオン交換樹脂に接触せしめることである。
【００１１】
本発明における処理法はバッチ式懸濁法による接触であっても効果は得られるが、通常カラム通液法が好ましく、該イオン交換樹脂をカラムに充填し上昇流または下降流によりアクリルアミド水溶液を接触させる方法がとられる。その際の通液速度に制限はないが、通常ＳＶ（空塔速度）が０．１以上２０（Ｈｒ−１）以下の範囲で処理するのが好ましく、１以上１０以下がさらに好ましい。通液温度はアクリルアミドが変質しない温度つまりは６０℃以下が好ましく、さらに低い温度であればより好ましいがその濃度のアクリルアミド飽和を示す温度より高いことが好ましい。
【００１２】
【実施例】
以下実施例で本発明をさらに詳細に説明する。以下においてｐｐｍあるいは％はアクリルアミド水溶液の重量基準である。
［実施例１］
イオン型をＮａ型に調整したアミノリン酸型中酸性イオン交換樹脂レバチットＯＣ１０６０（バイエル社製）を５０ｍｌ充填した内径１５ｍｍのガラス製カラムにアクリロニトリルの接触水和法により得られた銅イオン２４ｐｐｍを含む４０％アクリルアミド水溶液をＳＶが４（Ｈｒ−１）、下向流、温度３０℃で３０リットル通液した。カラム下部より流出した処理液中の銅イオン濃度は５ｐｐｂ以下であった。また処理液中にアクリルアミド重合物は検出されなかった。
【００１３】
［実施例２］
イオン型をＨ型に調整したアミノリン酸型中酸性イオン交換樹脂レバチットＯＣ１０６０（バイエル社製）を５０ｍｌ充填した内径１５ｍｍのガラス製カラムにアクリロニトリルの接触水和法により得られた銅イオン２８ｐｐｍを含む４０％アクリルアミド水溶液をＳＶが８（Ｈｒ−１）、下向流、温度３０℃で３０リットル通液した。カラム下部より流出した処理液中の銅イオン濃度は５ｐｐｂ以下であった。また処理液中にアクリルアミド重合物は検出されなかった。
【００１４】
［比較例１］
イオン交換樹脂を、イオン型をＨ型に調整した強酸性イオン交換樹脂レバチットＳＰ１１２（バイエル社製）としたほかは実施例１と同様にアクリルアミド水溶液を処理した。アクリルアミド水溶液を２リットル処理したときにアクリルアミドが重合しカラムが閉塞し処理が不能となった。
【００１５】
［比較例２］
イオン交換樹脂を、イオン型をＮａ型に調整した強酸性イオン交換樹脂レバチットＳＰ１１２（バイエル社製）としたほかは実施例１と同様にアクリルアミド水溶液を処理した。カラム下部より流出した処理液中の銅イオン濃度は４５５ｐｐｂであった。
【００１６】
［比較例３］
イオン交換樹脂を、イオン型をＨ型に調整したイミノジ酢酸型弱酸性イオン交換樹脂レバチットＴＰ２０７（バイエル社製）としたほかは実施例１と同様にアクリルアミド水溶液を処理した。カラム下部より流出した処理液中の銅イオン濃度は８５ｐｐｂであった。また試験後カラム内を点検したところアクリルアミドの重合物が見られた。
【００１７】
［比較例４］
イオン交換樹脂を、イオン型をＮａ型に調整したイミノジ酢酸型弱酸性イオン交換樹脂レバチットＴＰ２０７（バイエル社製）としたほかは実施例１と同様にアクリルアミド水溶液を処理した。カラム下部より流出した処理液中の銅イオン濃度は１６５ｐｐｂであった。
【００１８】
【発明の効果】
本発明によって、アクリロニトリルの接触水和反応によりアクリルアミド水溶液から長期、安定的に微量の銅を除去することが可能になり、このことはアクリルアミドの工業的生産にとって、きわめて大きな利益を与えるものである。[0001]
[Industrial applications]
The present invention relates to a copper removal method for purifying an aqueous acrylamide solution obtained by a contact hydration method of acrylonitrile.
[0002]
[Prior art]
Acrylamide is an industrially useful monomer used for the production of acrylamide-based polymers used for paper strength agents, flocculants, and the like, and for various uses.
A method for producing acrylamide by catalytic hydration of acrylonitrile in the presence of a copper metal catalyst is already well known. Therefore, it is inevitable that a trace amount of copper is eluted into the acrylamide-containing reaction solution obtained by using this copper-based catalyst. Therefore, when an attempt is made to produce a polymer using an aqueous acrylamide solution as a raw material, the copper dissolved therein inhibits the polymerization reaction, which significantly reduces the commercial value of the aqueous acrylamide solution. Therefore, in order to use an acrylamide aqueous solution obtained from the acrylamide reaction solution as a polymer raw material, it is necessary to remove dissolved copper. As a method for removing the dissolved copper, a method of treating with a strongly acidic cation exchange resin or a method of treating with a weakly acidic ion exchange resin of iminodiacetic acid type has been adopted.
[0003]
[Problems to be solved by the invention]
However, since acrylamide is highly reactive, it is extremely difficult to industrially remove copper dissolved in an aqueous acrylamide solution without polymerizing acrylamide. For example, when a strongly acidic ion exchange resin is used, the free acid type (abbreviated as H type) has a large copper removing ability, but the functional group is strongly acidic, so that highly reactive acrylamide is not polymerized. Inevitable. When this is a sodium salt type (abbreviated as Na type), polymerization of acrylamide can be avoided, but copper adsorption capacity is poor and sufficient removal performance cannot be obtained. When an iminodiacetic acid type weakly acidic ion exchange resin is used, if it is H type, it is weakly acidic, so that dissociation is weak and copper adsorption ability is weak. Further, in the case of the Na type, since the functional group is weakly acidic, there is a disadvantage that Na ions are eluted into the aqueous acrylamide solution.
[0004]
[Means for Solving the Problems]
That is, the present invention relates to a method for purifying an aqueous acrylamide solution, comprising treating an aqueous acrylamide solution obtained by a contact hydration method of acrylonitrile with an acidic ion exchange resin of aminophosphoric acid type.
The present invention provides a method of removing copper from an aqueous solution of acrylamide obtained by a contact hydration method of acrylonitrile using an aminophosphate type intermediate acid ion exchange resin. The use of a medium acidic ion exchange resin not only enables the removal of copper to an extremely low concentration due to its strong copper adsorption capacity, but also enables the polymerization of highly reactive acrylamide due to its moderate acidity. It is possible to carry out a very high degree of acrylamide purification, in which no hydrolysis occurs and no elution of Na ions or the like from the ion exchange resin.
[0005]
Hereinafter, the present invention will be described in detail.
The aqueous acrylamide solution used in the present invention can be obtained by a usual catalytic hydration method using acrylonitrile as a raw material. That is, acrylonitrile is charged together with water into a pressure-resistant reactor and reacted at a temperature of about 70 to 150 ° C. for about 1 to 3 hours in the presence of a metal copper catalyst. Since unreacted acrylonitrile remains in the obtained reaction solution, it is usually removed in advance.
[0006]
The acrylamide concentration of the acrylamide aqueous solution to be treated in the present invention is not limited, but the acrylamide concentration in the acrylamide aqueous solution usually obtained by the contact hydration method is about 20 to 60%, and the acrylamide aqueous solution in this range is preferably treated. Can be. Of course, it is applicable even if it is out of this range.
[0007]
The copper concentration in the acrylamide aqueous solution to be treated in the present invention is not limited, but the contact hydration method usually contains about 10 to 200 ppm of copper in the reaction solution, and such an acrylamide aqueous solution is preferably treated. Can be. Of course, it can be easily understood that the present invention can be suitably applied even if the concentration of copper is higher or lower.
[0008]
The medium-acid ion exchange resin used in the present invention is a medium-acid ion exchange resin of an aminophosphate type having a styrene-divinylbenzene copolymer as a base. (Manufactured by Bayer), Duolite C467 (manufactured by Rohm and Haas), and the like, and can be suitably used.
[0009]
The medium acidic ion exchange resin used in the present invention may be of H type or Na type. When used as the Na type, its adjustment method may be such that an aqueous solution of caustic soda in excess of the ion exchange capacity of the resin is brought into contact. Further, the resin after copper adsorption can be used as H-form by treating with a mineral acid, and can be converted into Na-form by performing the same treatment with an aqueous solution of caustic soda and reused.
[0010]
The treatment of the aqueous acrylamide solution in the present invention with an acidic ion exchange resin in an aminophosphoric acid type means that the aqueous solution is brought into contact with the ion exchange resin.
[0011]
The effect can be obtained even if the treatment method in the present invention is a contact by a batch suspension method.However, a column passing method is usually preferable, and the ion exchange resin is packed in a column and the acrylamide aqueous solution is contacted by an ascending flow or a descending flow. The method to make it take is taken. The liquid passing speed at this time is not limited, but the treatment is usually preferably performed at a SV (superficial velocity) of 0.1 to 20 (Hr -1 ), more preferably 1 to 10 (Hr -1 ). The liquid passing temperature is preferably a temperature at which acrylamide does not deteriorate, that is, 60 ° C. or lower, and more preferably a lower temperature, but preferably higher than a temperature at which the acrylamide is saturated at that concentration.
[0012]
【Example】
Hereinafter, the present invention will be described in more detail with reference to Examples. In the following, ppm or% is based on the weight of the aqueous acrylamide solution.
[Example 1]
A glass column having an inner diameter of 15 mm filled with 50 ml of aminophosphoric acid type acid ion exchange resin LEVATIT OC1060 (manufactured by Bayer) whose ion type has been adjusted to Na type contains 24 ppm of copper ions obtained by the contact hydration method of acrylonitrile. A 30% aqueous solution of acrylamide was passed through at a temperature of 30 ° C. in a downward flow at an SV of 4 (Hr −1 ). The copper ion concentration in the processing solution flowing out from the lower part of the column was 5 ppb or less. No acrylamide polymer was detected in the treatment liquid.
[0013]
[Example 2]
A glass column having an inner diameter of 15 mm filled with 50 ml of an aminophosphoric acid type acid ion exchange resin Levatit OC1060 (manufactured by Bayer) whose ion form has been adjusted to H form contains 28 ppm of copper ions obtained by the contact hydration method of acrylonitrile. A 30% aqueous acrylamide solution was passed through at a SV of 8 (Hr -1 ), in a downward flow at a temperature of 30 ° C. The copper ion concentration in the processing solution flowing out from the lower part of the column was 5 ppb or less. No acrylamide polymer was detected in the treatment liquid.
[0014]
[Comparative Example 1]
An acrylamide aqueous solution was treated in the same manner as in Example 1 except that the ion exchange resin was a strongly acidic ion exchange resin Levatit SP112 (manufactured by Bayer) whose ion type was adjusted to H type. When 2 liters of the acrylamide aqueous solution was treated, acrylamide was polymerized and the column was blocked, and the treatment became impossible.
[0015]
[Comparative Example 2]
An acrylamide aqueous solution was treated in the same manner as in Example 1 except that the ion exchange resin was a strongly acidic ion exchange resin Levatit SP112 (manufactured by Bayer) whose ion type was adjusted to Na type. The copper ion concentration in the processing solution flowing out from the lower part of the column was 455 ppb.
[0016]
[Comparative Example 3]
An aqueous acrylamide solution was treated in the same manner as in Example 1 except that the ion exchange resin was iminodiacetic acid type weak acid ion exchange resin Levatit TP207 (manufactured by Bayer) whose ion type was adjusted to H type. The copper ion concentration in the processing solution flowing out from the lower part of the column was 85 ppb. When the inside of the column was inspected after the test, a polymer of acrylamide was found.
[0017]
[Comparative Example 4]
An acrylamide aqueous solution was treated in the same manner as in Example 1 except that the ion exchange resin was iminodiacetic acid type weak acid ion exchange resin Levatit TP207 (manufactured by Bayer) whose ion type was adjusted to Na type. The copper ion concentration in the processing solution flowing out from the lower part of the column was 165 ppb.
[0018]
【The invention's effect】
According to the present invention, it is possible to stably remove trace amounts of copper from an aqueous solution of acrylamide by a catalytic hydration reaction of acrylonitrile for a long time, which has a great advantage for industrial production of acrylamide.
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28040694A JP3555997B2 (en) | 1994-11-15 | 1994-11-15 | Purification method of acrylamide aqueous solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP28040694A JP3555997B2 (en) | 1994-11-15 | 1994-11-15 | Purification method of acrylamide aqueous solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08143521A JPH08143521A (en) | 1996-06-04 |
| JP3555997B2 true JP3555997B2 (en) | 2004-08-18 |
Family
ID=17624597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP28040694A Expired - Fee Related JP3555997B2 (en) | 1994-11-15 | 1994-11-15 | Purification method of acrylamide aqueous solution |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3555997B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008247979A (en) * | 2007-03-29 | 2008-10-16 | Mitsui Chemicals Inc | Method for producing high-quality (meth)acrylamide polymer |
-
1994
- 1994-11-15 JP JP28040694A patent/JP3555997B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH08143521A (en) | 1996-06-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4895905A (en) | Gel-type chelating resins and a process for removal of multi-valent, alkaline earth or heavy metal cations from solutions | |
| US3984314A (en) | Process for selective removal and recovery of cyanide values by ion exchange | |
| AU621300B2 (en) | Alkylaminophosphonic chelating resins, their preparation and use in purifying brines | |
| JP3567206B2 (en) | Hydroxylamine purification method | |
| US4818773A (en) | Alkylaminophosphonic chelating resins, their preparation and use in purifying brines | |
| US3067007A (en) | Separation of strong polybasic acids from their salts | |
| US4150205A (en) | Composite ion exchange resins having low residual amounts of quaternary ammonium cation | |
| KR20010013064A (en) | Method for preparing an ultrapure hydrogen peroxide solution by ion exchange in the presence of ion acetate | |
| JP3555997B2 (en) | Purification method of acrylamide aqueous solution | |
| US4405574A (en) | Removal of Mg++ and Ca++ ions from NaCl brine | |
| US2734915A (en) | Acrylic acid | |
| US4108893A (en) | Purification of an aqueous solution of acrylamide | |
| US4522951A (en) | Removal of Mg++ and Ca++ ions from NaCl brine | |
| JP3529113B2 (en) | Method for removing impurities from hydrazine hydrate | |
| KR960000480B1 (en) | Process for demineralizing a sweet juices | |
| JP3476226B2 (en) | Purification method of methacrylamide aqueous solution | |
| JPS581108B2 (en) | Acrylonitrile purification method | |
| JP4476367B2 (en) | Purification method of acrylamide aqueous solution | |
| EP0691889B1 (en) | Resin regeneration process | |
| JPS61201611A (en) | Purification method for aqueous solution of phosphate | |
| JP2001131221A (en) | Method for production of ionic polymer compound | |
| JPH0545299B2 (en) | ||
| US4302600A (en) | Process for the purification of an aqueous acrylamide solution | |
| JPS6343381B2 (en) | ||
| SU1087514A1 (en) | Method for purifying aqueous acrylamide solution |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20040511 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20040511 |
|
| R150 | Certificate of patent or registration of utility model |
Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20080521 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20090521 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100521 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100521 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110521 Year of fee payment: 7 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120521 Year of fee payment: 8 |
|
| LAPS | Cancellation because of no payment of annual fees |