JP2003146936A - Method for producing (meth)acrylic acid compound - Google Patents
Method for producing (meth)acrylic acid compoundInfo
- Publication number
- JP2003146936A JP2003146936A JP2001341348A JP2001341348A JP2003146936A JP 2003146936 A JP2003146936 A JP 2003146936A JP 2001341348 A JP2001341348 A JP 2001341348A JP 2001341348 A JP2001341348 A JP 2001341348A JP 2003146936 A JP2003146936 A JP 2003146936A
- Authority
- JP
- Japan
- Prior art keywords
- acrylic acid
- meth
- temperature
- storage tank
- heat exchanger
- 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.)
- Pending
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
【0001】[0001]
【発明の属する技術分野】本発明は、(メタ)アクリル
酸類を製造する方法に係り、特に蒸留塔で精製された精
製(メタ)アクリル酸類の凝縮液を貯蔵する貯蔵タンク
において、当該貯蔵タンクに付設されている熱交換器の
伝熱面積をコンパクトすることにより設備費の削減を図
ったものである。なお、本発明で使用する(メタ)アク
リル酸類とはアクリル酸及びメタクリル酸(以下「(メ
タ)アクリル酸」と云う。)と当該(メタ)アクリル酸
のエステルを含めた用語である。TECHNICAL FIELD The present invention relates to a method for producing (meth) acrylic acid, and more particularly to a storage tank for storing a condensate of purified (meth) acrylic acid purified in a distillation column. By reducing the heat transfer area of the attached heat exchanger, the equipment cost is reduced. The (meth) acrylic acid used in the present invention is a term including acrylic acid and methacrylic acid (hereinafter referred to as “(meth) acrylic acid”) and the ester of the (meth) acrylic acid.
【0002】[0002]
【従来の技術】従来、接触気相酸化によって(メタ)ア
クリル酸類を製造するプロセスにおいては、(メタ)ア
クリル酸類を分離或いは精製して、一般には最終の精製
塔(蒸留塔)の塔頂より製品が得られる。この製品は、
品質確認のための品質確認用タンクに送出され、製品と
しての検査を実施した後に貯蔵タンクに保管される。場
合によっては直接製品を貯蔵タンクに送出、保管され
る。2. Description of the Related Art Conventionally, in a process for producing (meth) acrylic acid by catalytic gas phase oxidation, (meth) acrylic acid is separated or purified, and generally, it is obtained from the top of a final purification column (distillation column). The product is obtained. This product is
It is sent to a quality confirmation tank for quality confirmation, and after being inspected as a product, it is stored in a storage tank. In some cases, the product is directly sent to a storage tank and stored.
【0003】[0003]
【発明が解決しようとする課題】易重合性物質である
(メタ)アクリル酸類を製造及び/又は精製する場合に
おいて、その製品を保管する際に、重合防止、爆鳴気形
成回避、さらにアクリル酸においてはアクリル酸の2量
体の生成抑制のために、当該製品を保管する貯蔵タンク
は比較的低温状態に管理・維持する必要がある。このた
め、貯蔵タンクには温度管理(主に冷却状態の維持)の
ための付帯設備が設けられている。当該貯蔵タンクの付
帯設備としてはタンク内に冷却コイルを内挿或いは外部
に熱交換器を設置して温度管理を行っていた。When manufacturing and / or purifying (meth) acrylic acid which is an easily polymerizable substance, when the product is stored, polymerization is prevented, detonation is avoided, and acrylic acid is further used. In order to suppress the formation of acrylic acid dimer, it is necessary to manage and maintain the storage tank for storing the product at a relatively low temperature. For this reason, the storage tank is provided with auxiliary equipment for temperature control (mainly maintaining the cooling state). As auxiliary equipment of the storage tank, a cooling coil is inserted in the tank or a heat exchanger is installed outside to control the temperature.
【0004】一方、それぞれのプロセスにおいて精製塔
の塔頂より得られる製品は、易重合性であるため、運転
温度を低下させるるために通常減圧下での蒸留が行われ
る。そして塔頂からのガスは凝縮器を通過する間に冷却
されて製品である凝縮液が得られる。この凝縮液の温度
は一般に工業的な用役条件から約40℃程度となってい
る。次いで、この製品の凝縮液を貯蔵タンクに移送して
保管するためには、貯蔵タンク内の凝縮液の温度を上記
温度以下の比較的低温状態に管理・維持する必要があ
り、従来この温度管理・維持のための付帯設備が比較的
大きくまた設備費も嵩んでいた。On the other hand, since the product obtained from the top of the purification column in each process is easily polymerized, distillation is usually performed under reduced pressure to lower the operating temperature. Then, the gas from the top of the column is cooled while passing through the condenser to obtain a condensate as a product. The temperature of this condensate is generally about 40 ° C. due to industrial service conditions. Next, in order to transfer the condensate of this product to the storage tank and store it, it is necessary to control and maintain the temperature of the condensate in the storage tank at a relatively low temperature below the above temperature.・ The auxiliary equipment for maintenance was relatively large and the equipment cost was high.
【0005】[0005]
【課題を解決する手段】本発明は、(メタ)アクリル酸
類の製造方法において、(メタ)アクリル酸類を貯蔵す
る貯蔵タンクの付帯設備をコンパクトにして設備費の削
減を図った(メタ)アクリル酸類の製造方法を提供する
ものであって、その要旨は、(1)(メタ)アクリル酸
類を製造及び/又は精製するプロセスにおいて、得られ
た精製(メタ)アクリル酸類を貯蔵タンクへ供給する際
の温度を、当該貯蔵タンク内に貯留された精製(メタ)
アクリル酸類の温度以下に制御することを特徴とする
(メタ)アクリル酸類の製造方法である。
(2)精製(メタ)アクリル酸類が塔頂留出物の凝縮液
であり、かつその凝縮液を貯蔵タンクに供給するライン
系中に熱交換器を組み込んでなる上記(1)の(メタ)
アクリル酸類の製造方法である。
(3)貯蔵タンクへ供給する精製(メタ)アクリル酸類
の温度が0〜35℃である上記(1)又は(2)の(メ
タ)アクリル酸類の製造方法である。According to the present invention, in a method for producing (meth) acrylic acid, the auxiliary equipment of a storage tank for storing (meth) acrylic acid is made compact to reduce the equipment cost. (1) In the process of producing and / or purifying (meth) acrylic acid, the purified (meth) acrylic acid obtained is supplied to a storage tank. Refining temperature (meta) stored in the storage tank
A method for producing (meth) acrylic acid, which is characterized by controlling the temperature to be equal to or lower than the temperature of acrylic acid. (2) Purified (meth) acrylic acid is a condensate of overhead distillate, and a heat exchanger is incorporated in a line system for supplying the condensate to a storage tank.
It is a method for producing acrylic acids. (3) The method for producing (meth) acrylic acid according to (1) or (2), wherein the temperature of the purified (meth) acrylic acid supplied to the storage tank is 0 to 35 ° C.
【0006】[0006]
【発明の実施の形態】本発明の(メタ)アクリル酸類の
製造方法を添付図面に基づいて説明する。図1は本発明
の(メタ)アクリル酸類の製造方法のフローシートであ
る。BEST MODE FOR CARRYING OUT THE INVENTION The method for producing (meth) acrylic acid according to the present invention will be described with reference to the accompanying drawings. FIG. 1 is a flow sheet of the method for producing (meth) acrylic acid according to the present invention.
【0007】先ず最初に、図1に基づいて本発明の製造
方法に使用する製造装置の概要を説明する。Aは精製塔
であって、当該精製塔Aには精製される液の供給ライン
1が取付けられている。Bはリボイラーであって、当該
リボイラーBの流入側は精製塔Aの塔底に取付けられて
いる塔底抜き出しライン2の途中から分岐されたリボイ
ラー循環ライン3が接続されており、またその流出側は
リボイラー循環ライン4を介して精製塔Aの下側壁に接
続されている。First, an outline of a manufacturing apparatus used in the manufacturing method of the present invention will be described with reference to FIG. A is a purification tower, and a supply line 1 for the liquid to be purified is attached to the purification tower A. B is a reboiler, the inflow side of which is connected to a reboiler circulation line 3 branched from the middle of a bottom extraction line 2 attached to the bottom of the purification column A, and its outflow side Is connected to the lower side wall of the purification tower A via a reboiler circulation line 4.
【0008】Cは凝縮器であって、当該凝縮器Cの流入
側は精製塔Aの塔頂に取付けられた塔頂ガスライン5に
接続されており、その流出側はラインを介して還流槽E
の流入側に接続されている。また、還流槽Eの流出側は
還流ライン6によって精製塔Aの上側壁に接続されてお
り、この還流ライン6の途中には製品抜き出しライン7
が分岐して設けられている。Dはベントコンデンサーで
あって、当該ベントコンデンサーDの流入側はベントラ
イン8を介して上記還流槽Eに接続されている。C is a condenser, the inflow side of the condenser C is connected to a top gas line 5 attached to the top of the purification tower A, and the outflow side thereof is connected to the reflux tank via the line. E
Is connected to the inflow side of. Further, the outflow side of the reflux tank E is connected to the upper side wall of the refining tower A by a reflux line 6, and in the middle of this reflux line 6, a product extraction line 7
Are diverged. D is a vent condenser, and the inflow side of the vent condenser D is connected to the reflux tank E via a vent line 8.
【0009】Fは製品温度調整用熱交換器であって、当
該製品温度調整用熱交換器Fは本発明のポイントをなす
主要装置で、製品温度調整用熱交換器Fの流入側は製品
抜き出しライン7に接続されており、その流出側は品質
確認用タンクKを介して貯蔵タンクGの流入側に接続さ
れている。この製品温度調整用熱交換器Fは特に特殊形
式のものでなく固定管板式熱交換器、スパイラル式熱交
換器、コンパブロック型熱交換器及びプレート型熱交換
器等種々形式のものが使用できる。また、品質確認用タ
ンクKは本例示では製品温度調整用熱交換器Fの流出側
と貯蔵タンクGの流入側との間の製品抜き出しライン7
中に設置されているが、製品温度調整用熱交換器Fの流
入側の製品抜き出しライン7中に設置してもよく、場合
によっては当該品質確認用タンクKを省略することもで
きる。F is a heat exchanger for adjusting the product temperature, and the heat exchanger F for adjusting the product temperature is a main device which is the main point of the present invention. The inflow side of the heat exchanger for adjusting the product temperature F is withdrawn from the product. It is connected to the line 7, and its outflow side is connected to the inflow side of the storage tank G via the quality confirmation tank K. This product temperature adjusting heat exchanger F is not of a special type, and various types such as a fixed tube plate type heat exchanger, a spiral type heat exchanger, a compactor block type heat exchanger and a plate type heat exchanger can be used. . Further, the quality confirmation tank K is, in this example, the product extraction line 7 between the outflow side of the product temperature adjustment heat exchanger F and the inflow side of the storage tank G.
Although installed inside, it may be installed in the product extraction line 7 on the inflow side of the product temperature adjustment heat exchanger F, and in some cases, the quality confirmation tank K may be omitted.
【0010】上記貯蔵タンクGの内部には液温調整用コ
イルJが内蔵されている。Hはタンク液温調節用熱交換
器であって、当該タンク液温調節用熱交換器Hの流入側
は貯蔵タンクGの流出側にタンク抜き出しライン10及
び循環ライン12を介して接続されおり、またその流出
側はラインによって貯蔵タンクGの側壁に接続されてい
る。このように貯蔵タンクGに付設される液温調整用コ
イルJ又はタンク液温調節用熱交換器Hは両方付設して
も良いが、どちらか一方のみが付設されるのが一般的で
ある。また、タンク抜き出しライン10と循環ライン1
2との結合部から出荷等抜き出しライン11が分岐して
設けられている。A liquid temperature adjusting coil J is built in the storage tank G. H is a heat exchanger for adjusting the temperature of the tank liquid, and the inflow side of the heat exchanger H for adjusting the tank liquid temperature is connected to the outflow side of the storage tank G via a tank extraction line 10 and a circulation line 12. The outflow side is connected to the side wall of the storage tank G by a line. Thus, both the liquid temperature adjusting coil J and the tank liquid temperature adjusting heat exchanger H attached to the storage tank G may be attached, but it is general that only one of them is attached. In addition, the tank extraction line 10 and the circulation line 1
A line 11 for withdrawing products such as shipments is provided so as to branch from the joint with the unit 2.
【0011】次に、同じく図1に基づいて本発明の製造
方法の製造工程の概要についてを説明する。供給ライン
1より精製塔A内に供給された処理液は精製操作を経
て、その一部が当該精製塔Aの塔底に流下する。この塔
底液は、塔底抜き出しライン2に導かれ、その一部はリ
ボイラー還流ライン3よりリボイラーBを経由してリボ
イラー還流ライン4より精製塔A内に戻され、残りは塔
底抜き出しライン2より外部に排出される。当該外部に
排出された塔底液は、有価物を多く含んでいるため、場
合によっては精製系に戻されたり或いは有価物回収設備
に供給される。回収されない場合は廃棄物として処理さ
れる。Next, an outline of the manufacturing process of the manufacturing method of the present invention will be described with reference to FIG. The treatment liquid supplied from the supply line 1 into the purification tower A undergoes a purification operation, and a part thereof flows down to the bottom of the purification tower A. This bottom liquid is introduced into the bottom extraction line 2, part of it is returned from the reboiler reflux line 3 to the reboiler reflux line 4 through the reboiler B into the purification column A, and the rest is removed from the bottom bottom extraction line 2 More discharged to the outside. Since the bottom liquid discharged to the outside contains a large amount of valuables, it is returned to the purification system or supplied to the valuables recovery facility in some cases. If not collected, it will be treated as waste.
【0012】一方、精製塔A内に供給された処理液は精
製されて、当該精製塔Aの塔頂よりガス状となって塔頂
ガスライン5より凝縮器Cに導かれる。当該凝縮器Cよ
ってガスは冷却されて約40℃の精製(メタ)アクリル
酸類の凝縮液となり還流槽Eを経由して、その一部は還
流ライン6より精製塔A内に戻され、残りの凝縮液は製
品抜き出しライン7に導かれる。また、ベントライン8
によって還流槽EからベントコンデンサーDへ導かれた
ベントガスは、ここで冷却されガス中の有価物を回収し
た後、残りは精製塔A内の圧力を調整する真空系統等
(図示せず)に導かれる。On the other hand, the treatment liquid supplied into the purification tower A is purified, becomes a gas from the top of the purification tower A, and is introduced into the condenser C from the top gas line 5. The gas is cooled by the condenser C to be a condensed liquid of purified (meth) acrylic acid at about 40 ° C., and a part of the condensed liquid is returned from the reflux line 6 into the purification tower A through the reflux tank E, and the remaining The condensate is guided to the product withdrawal line 7. Also, vent line 8
The vent gas led from the reflux tank E to the vent condenser D is cooled here, and after recovering valuable substances in the gas, the rest is introduced to a vacuum system or the like (not shown) for adjusting the pressure in the purification tower A. Get burned.
【0013】ところで、製品抜き出しライン7に導かれ
約40℃の凝縮液は、製品温度調整用熱交換器Fに送ら
れる。ここで凝縮液は更に温度調整された後、品質確認
用タンクKを経由して貯蔵タンクGに供給される。貯蔵
タンクGに供給される精製(メタ)アクリル酸類の温度
は0〜35℃、更に好ましくは5〜35℃である。な
お、アクリル酸のように凝固点が13℃の値を有するも
のについては、凝固点以上の例えば15〜25℃とする
ことが好ましい。(メタ)アクリル酸類が貯留される貯
蔵タンクG内の温度は、その貯留される種別によって最
適値が異なるが一般的に0〜35℃である。なお、この
温度についても上記同様に凝固点の温度を考慮して定め
ればよい。By the way, the condensate of about 40 ° C. guided to the product extraction line 7 is sent to the product temperature adjusting heat exchanger F. Here, the temperature of the condensate is further adjusted and then supplied to the storage tank G via the quality confirmation tank K. The temperature of the purified (meth) acrylic acid supplied to the storage tank G is 0 to 35 ° C, more preferably 5 to 35 ° C. For acrylic acid having a freezing point of 13 ° C., it is preferable to set the freezing point to, for example, 15 to 25 ° C. or higher. The temperature inside the storage tank G in which the (meth) acrylic acid is stored is generally 0 to 35 ° C. although the optimum value varies depending on the type of storage. It should be noted that this temperature may be determined in consideration of the temperature of the freezing point as in the above.
【0014】上記貯蔵タンクGに供給される凝縮液の温
度が上記の好適な温度範囲になるように製品温度調整用
熱交換器Fで温度制御して当該熱交換器Fから送り出
す。製品温度調整用熱交換器Fで使用される冷却媒体
は、上水、工業用水、再冷水、ボイラー水、スチームコ
ンデンセート水等に代表される水、海水、有機媒体等の
冷媒を、一種以上使用して凝縮液を所定の温度に制御す
る。The condensate supplied to the storage tank G is temperature-controlled by the product temperature adjusting heat exchanger F so that the temperature of the condensate is in the above-mentioned suitable temperature range, and the product is sent out from the heat exchanger F. As the cooling medium used in the product temperature adjustment heat exchanger F, one or more refrigerants such as tap water, industrial water, re-cooled water, boiler water, steam condensate water, and other water, seawater, organic media, etc. are used. Then, the condensate is controlled to a predetermined temperature.
【0015】貯蔵タンクG内に貯留された精製(メタ)
アクリル酸類は当該タンクG内に内蔵されている液温調
整用コイルJにより、或いは当該タンクG内に貯留され
た精製(メタ)アクリル酸類の一部を外部に付設されて
いるタンク液温調節用熱交換器Hにタンク抜き出しライ
ン10及び循環ライン12を介して循環させることによ
って、当該貯蔵タンクG内に貯留された精製(メタ)ア
クリル酸類を所定の温度である0〜35℃に温度制御す
るのがよい。一方、所定の液温に制御された貯蔵タンク
G内の精製(メタ)アクリル酸類は、タンク抜き出しラ
イン10及び出荷等抜き出しライン11を介して製品と
して出荷される。Purification (meta) stored in the storage tank G
Acrylic acid is used for adjusting the liquid temperature of the tank by the liquid temperature adjusting coil J built in the tank G or a part of the purified (meth) acrylic acid stored in the tank G is attached to the outside. By circulating the heat exchanger H through the tank extraction line 10 and the circulation line 12, the temperature of the purified (meth) acrylic acid stored in the storage tank G is controlled to a predetermined temperature of 0 to 35 ° C. Is good. On the other hand, the purified (meth) acrylic acid in the storage tank G, which is controlled to a predetermined liquid temperature, is shipped as a product through the tank extraction line 10 and the extraction line 11 such as shipping.
【0016】本発明の製造方法の主要ポイントは、凝縮
器Cで凝縮された新たな凝縮液を直接に貯蔵タンクGに
供給するのでなく、当該貯蔵タンクGの前工程に設置さ
れた製品温度調整用熱交換器Fを通過させることによっ
て凝縮液を予め貯蔵タンクGに貯留された精製(メタ)
アクリル酸類の温度以下に冷却して貯蔵タンクGに供給
するものである。ここで、伝熱量Q=AhΔTの式で表
される(Aは伝熱面積、hは熱伝達率、ΔTは温度差で
ある)。従って、従来方法のように、凝縮器Cで凝縮さ
れた新たな凝縮液を貯蔵タンクGに直接に供給して、貯
蔵タンクG内に貯留された精製(メタ)アクリル酸類と
混合させ、当該混合された精製(メタ)アクリル酸類を
所定温度に制御する為に冷却するには、その制御の温度
差ΔTが小さいために大きな伝熱面積Aを具備した熱交
換器等が必要となる。一方、本発明の如く製品温度調整
用熱交換器Fを別個に設置することにより、当該熱交換
器Fの入口凝縮液温は凝縮器Cの出口凝縮液温の約40
℃であり、また当該熱交換器Fの出口凝縮液温は貯蔵タ
ンクG内に貯留された精製(メタ)アクリル酸類の温度
以下の低い温度に設定できる。したかって、熱交換器F
の入口及び出口の温度差ΔTが大きく取ることができる
ので、熱交換器Fの伝熱面積Aを小さくても所定の伝熱
量Qを得ることができる。この結果、貯蔵タンクG内に
貯留された精製(メタ)アクリル酸類の温度制御のため
に必要な熱交換器全体の伝熱面積を小さくすることが可
能となった。The main point of the manufacturing method of the present invention is not to directly supply the new condensate condensed in the condenser C to the storage tank G, but to adjust the temperature of the product installed in the preceding step of the storage tank G. By refining the condensate in the storage tank G in advance by passing it through the heat exchanger F (meta)
It is cooled below the temperature of acrylic acids and supplied to the storage tank G. Here, the heat transfer amount Q = AhΔT is represented (A is a heat transfer area, h is a heat transfer coefficient, and ΔT is a temperature difference). Therefore, as in the conventional method, the new condensate condensed in the condenser C is directly supplied to the storage tank G and mixed with the purified (meth) acrylic acid stored in the storage tank G, and the mixing is performed. In order to cool the purified (meth) acrylic acid thus produced to control it at a predetermined temperature, a heat exchanger or the like having a large heat transfer area A is required because the temperature difference ΔT in the control is small. On the other hand, by separately installing the product temperature adjusting heat exchanger F as in the present invention, the inlet condensate temperature of the heat exchanger F is about 40 times the outlet condensate temperature of the condenser C.
The temperature of the outlet condensate of the heat exchanger F can be set to a low temperature equal to or lower than the temperature of the purified (meth) acrylic acid stored in the storage tank G. Therefore, the heat exchanger F
Since a large temperature difference ΔT between the inlet and the outlet can be obtained, a predetermined amount of heat transfer Q can be obtained even if the heat transfer area A of the heat exchanger F is small. As a result, it is possible to reduce the heat transfer area of the entire heat exchanger required for controlling the temperature of the purified (meth) acrylic acid stored in the storage tank G.
【0017】[0017]
【実施例】実施例1
図1において、精製塔A内でアクリル酸を精製し、これ
を凝縮器C及び還流槽Eを通過させて得た40℃の凝縮
液を、製品抜き出しライン7によって1275kg/h
rの量を製品温度調整用熱交換器F内に流入して熱交換
を行って20℃に冷却して流出し、この凝縮液を温度が
常に20℃に維持されるようにタンク液温調節用熱交換
器Hによって温度調整された当該貯蔵タンクG内に供給
した後、出荷等抜き出しライン11を介して製品として
出荷した。製品温度調整用熱交換器Fは伝熱面積が4.
5m2のスパイラル式熱交換器であって水温15℃の冷
却水を使用した。また、タンク液温調節用熱交換器Hは
伝熱面積が17.5m2で同様にスパイラル式熱交換器
で水温15℃の冷却水を使用した。
比較例1
実施例1に於ける製品温度調整用熱交換器Fを設置しな
い場合、貯蔵タンクG内に貯留された精製(メタ)アク
リル酸類の温度が常に20℃に維持するためには、タン
ク液温調節用熱交換器Hの伝熱面積は25.5m2必要
であった。従って、実施例1の熱交換器の全体伝熱面積
が22m2(4.5+17.5)に対し、比較例1の熱
交換器の伝熱面積は25.5m2が必要であった。Example 1 In FIG. 1, acrylic acid was purified in a purification tower A and passed through a condenser C and a reflux tank E to obtain a condensate at 40 ° C. / H
The amount of r flows into the product temperature adjusting heat exchanger F to perform heat exchange, cool to 20 ° C and flow out, and adjust the tank liquid temperature so that the temperature of this condensate is always maintained at 20 ° C. After being supplied into the storage tank G whose temperature was adjusted by the heat exchanger H for use, the product was shipped as a product through the extraction line 11 for shipping and the like. Heat transfer area F for product temperature adjustment has a heat transfer area of 4.
A 5 m 2 spiral heat exchanger with cooling water having a water temperature of 15 ° C. was used. Further, the tank liquid temperature adjusting heat exchanger H had a heat transfer area of 17.5 m 2 and was similarly a spiral heat exchanger using cooling water having a water temperature of 15 ° C. Comparative Example 1 In the case where the product temperature adjusting heat exchanger F in Example 1 is not installed, in order to always maintain the temperature of the purified (meth) acrylic acid stored in the storage tank G at 20 ° C., The heat transfer area of the liquid temperature adjusting heat exchanger H was required to be 25.5 m 2 . Therefore, the total heat transfer area of the heat exchanger of Example 1 was 22 m 2 (4.5 + 17.5), whereas the heat transfer area of the heat exchanger of Comparative Example 1 was 25.5 m 2 .
【0018】[0018]
【発明の効果】本発明方法を使用すれば、製品の保管或
いは出荷の為に設置された貯蔵タンク内に貯留された精
製(メタ)アクリル酸液体を適温に制御するために設け
られる熱交換器の伝熱面積は、従来より小さくできるの
で装置全体がコンパクトとなり設備費の削減となる。精
製塔及び凝縮器の工程を経て凝縮された新たな凝縮液を
貯蔵タンクに供給する際に、当該凝縮液温は貯蔵タンク
に貯留された精製(メタ)アクリル酸類の温度以下に低
く温度制御してあるので、貯蔵タンクの精製(メタ)ア
クリル酸類の温が一時的にも上昇することがなく、当該
貯蔵タンク内での精製(メタ)アクリル酸類の重合体発
生が抑制される。特に、アクリル酸の製造方法において
は、アクリル酸の2量体の生成抑制になる。According to the method of the present invention, the heat exchanger provided for controlling the temperature of the purified (meth) acrylic acid liquid stored in the storage tank installed for storing or shipping the product at an appropriate temperature. Since the heat transfer area can be made smaller than the conventional one, the entire device can be made compact and the equipment cost can be reduced. When supplying a new condensate condensed through the steps of the purification tower and the condenser to the storage tank, the temperature of the condensate is controlled to be lower than the temperature of the purified (meth) acrylic acid stored in the storage tank. Therefore, the temperature of the purified (meth) acrylic acid in the storage tank does not rise even temporarily, and the generation of the polymer of the purified (meth) acrylic acid in the storage tank is suppressed. Particularly, in the method for producing acrylic acid, the formation of a dimer of acrylic acid is suppressed.
【図1】本発明の(メタ)アクリル酸類の製造方法のフ
ローシート。FIG. 1 is a flow sheet of a method for producing (meth) acrylic acid according to the present invention.
A…精製塔、B…リボイラー、C…凝縮器、D…ベント
コンデンサー、E…還流槽、F…製品温度調整用熱交換
器、G…貯蔵タンク、H…タンク液温調節用熱交換器、
J…液温調整用コイル、K…品質確認用タンク、1…精
製される液の供給ライン、11…出荷等抜き出しライ
ン、A ... Purification tower, B ... Reboiler, C ... Condenser, D ... Vent condenser, E ... Reflux tank, F ... Product temperature adjusting heat exchanger, G ... Storage tank, H ... Tank liquid temperature adjusting heat exchanger,
J ... Coil for liquid temperature adjustment, K ... Tank for quality confirmation, 1 ... Supply line of liquid to be purified, 11 ...
───────────────────────────────────────────────────── フロントページの続き (72)発明者 保坂 浩親 三重県四日市市東邦町1番地 三菱化学株 式会社内 (72)発明者 鈴木 芳郎 三重県四日市市東邦町1番地 三菱化学株 式会社内 Fターム(参考) 4H006 AA02 AA05 BD84 BS10 ─────────────────────────────────────────────────── ─── Continued front page (72) Inventor Hirochika Hosaka 1 Toho-cho, Yokkaichi-shi, Mie Mitsubishi Chemical Corporation Inside the company (72) Inventor Yoshiro Suzuki 1 Toho-cho, Yokkaichi-shi, Mie Mitsubishi Chemical Corporation Inside the company F-term (reference) 4H006 AA02 AA05 BD84 BS10
Claims (3)
精製するプロセスにおいて、得られた精製(メタ)アク
リル酸類を貯蔵タンクへ供給する際の温度を、当該貯蔵
タンク内に貯留された精製(メタ)アクリル酸類の温度
以下に制御することを特徴とする(メタ)アクリル酸類
の製造方法。1. In the process of producing and / or purifying (meth) acrylic acid, the temperature at which the obtained purified (meth) acrylic acid is supplied to a storage tank is the refining ((meth) acrylic acid stored in the storage tank. A method for producing (meth) acrylic acid, which comprises controlling the temperature to be equal to or lower than the temperature of (meth) acrylic acid.
の凝縮液であり、かつその凝縮液を貯蔵タンクに供給す
るライン系中に熱交換器を組み込んでなる請求項1記載
の(メタ)アクリル酸類の製造方法。2. The method according to claim 1, wherein the purified (meth) acrylic acid is a condensate of overhead distillate, and a heat exchanger is incorporated in a line system for supplying the condensate to a storage tank. Method for producing (meth) acrylic acid.
リル酸類の温度が0〜35℃である請求項1又は2に記
載の(メタ)アクリル酸類の製造方法。3. The method for producing (meth) acrylic acid according to claim 1, wherein the temperature of the purified (meth) acrylic acid supplied to the storage tank is 0 to 35 ° C.
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001341348A JP2003146936A (en) | 2001-11-07 | 2001-11-07 | Method for producing (meth)acrylic acid compound |
PCT/JP2002/011468 WO2003040002A1 (en) | 2001-11-07 | 2002-11-01 | Storage tank for easily polymerizable compound and storage method |
CNB028219597A CN1281572C (en) | 2001-11-07 | 2002-11-01 | Storage tank for easily polymerizable compound and method of storage |
CNB2004100587360A CN1297454C (en) | 2001-11-07 | 2002-11-01 | Storage tank for easily polymerizable compound and method of storage |
CNB2004100587375A CN100334382C (en) | 2001-11-07 | 2002-11-01 | Storage tank for easily polymerizable compound and method of storage |
CNB200410058738XA CN1260199C (en) | 2001-11-07 | 2002-11-01 | Storage tank for easily polymerizable compound and method of storage |
US10/840,612 US7188639B2 (en) | 2001-11-07 | 2004-05-07 | Storage tank for easily polymerizable compound and method of storage |
US11/133,184 US7241919B2 (en) | 2001-11-07 | 2005-05-20 | Storage tank for easily polymerizable compound and method of storage |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001341348A JP2003146936A (en) | 2001-11-07 | 2001-11-07 | Method for producing (meth)acrylic acid compound |
Publications (1)
Publication Number | Publication Date |
---|---|
JP2003146936A true JP2003146936A (en) | 2003-05-21 |
Family
ID=19155381
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP2001341348A Pending JP2003146936A (en) | 2001-11-07 | 2001-11-07 | Method for producing (meth)acrylic acid compound |
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Country | Link |
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JP (1) | JP2003146936A (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6968872B2 (en) | 2003-10-07 | 2005-11-29 | Mitsubishi Chemical Corporation | Process for recovering liquid chemical products in chemical production facility |
-
2001
- 2001-11-07 JP JP2001341348A patent/JP2003146936A/en active Pending
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6968872B2 (en) | 2003-10-07 | 2005-11-29 | Mitsubishi Chemical Corporation | Process for recovering liquid chemical products in chemical production facility |
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