JP6739829B1 - Separation apparatus and method for highly efficient purification treatment of waste oil residual liquid in chemical industry - Google Patents
Separation apparatus and method for highly efficient purification treatment of waste oil residual liquid in chemical industry Download PDFInfo
- Publication number
- JP6739829B1 JP6739829B1 JP2020011632A JP2020011632A JP6739829B1 JP 6739829 B1 JP6739829 B1 JP 6739829B1 JP 2020011632 A JP2020011632 A JP 2020011632A JP 2020011632 A JP2020011632 A JP 2020011632A JP 6739829 B1 JP6739829 B1 JP 6739829B1
- Authority
- JP
- Japan
- Prior art keywords
- valve
- oil
- tank
- liquid
- 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.)
- Active
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
Abstract
【課題】化学工業における汚油残液の高効率浄化処理用の分離装置及び方法を提供し、これら汚油残液を集中して回収し効率よく浄化処理することを目的とする。【解決手段】貯蔵設備、蒸留分離設備、静的混合設備、重力沈降設備を備えた装置である。易揮発性軽質／難揮発性重質の汚油残液原料をそれぞれ貯蔵設備で、重力により自然沈降し、連続又は間欠方式で気体炭化水素及び沈降液に分離する。貯蔵設備からの清澄液を、蒸留−水洗又は水洗−蒸留の２種の異なる技術手段に従って分離処理する。汚油残液の性質に応じて異なる操作プロセスを切り替えることにより、汚油残液の利用率を向上させ、汚油残液における高品質成分を十分に利用し、環境汚染を低減させる。また、塔頂留分油が原料に戻るためのパイプラインを増設することによって、正常に分離処理できるように汚油残液組成の性質を調整する。【選択図】図１PROBLEM TO BE SOLVED: To provide a separation device and a method for highly efficient purification treatment of waste oil residual liquid in the chemical industry, and to collect these waste oil residual liquid in a concentrated manner and efficiently purify them. The apparatus includes a storage facility, a distillation separation facility, a static mixing facility, and a gravity settling facility. Easily volatile light/hardly volatile heavy oil residual liquid raw materials are naturally settled by gravity in storage facilities and separated into gaseous hydrocarbons and settling liquids in a continuous or intermittent manner. The clarified liquid from the storage facility is separated according to two different technical means: distillation-washing or washing-distillation. By switching between different operation processes depending on the properties of the residual oil spill, the utilization rate of the residual oil spill is improved, the high quality components in the residual oil spill are fully utilized, and environmental pollution is reduced. In addition, by adding a pipeline for returning the overhead distillate oil to the raw material, the properties of the waste oil residual liquid composition are adjusted so that the separation process can be performed normally. [Selection diagram] Figure 1
Description
本発明は、石油化学工業生産の技術分野に関し、より具体的には、石油化学工業の生産過程における汚油残液の高効率浄化処理用の装置に関する。 TECHNICAL FIELD The present invention relates to the technical field of petrochemical industry production, and more specifically, to an apparatus for highly efficient purification treatment of waste oil residual liquid in the production process of petrochemical industry.
中国の石油化学産業の急速な発展に伴い、生産過程においてさまざまな汚油残液が不可避的に発生する。分解によりエチレンを製造する大型装置では、分解過程に高温タールが存在し、その下流の関連装置は、重合過程においてさまざまな汚油残液を発生させる。これら汚油残液は、物理的及び化学的性質がさまざまであり、コロイド・アスファルテン、液状ポリマー、オレフィン基を有する芳香環化合物、さらに使用済みの触媒粉末や微小炭素顆粒を含む。また、安全及び環境保護政策の厳格化に伴い、これら廃油が、企業内で無害化処理されて利用できなければ、企業の持続可能な発展を制限してしまうことになる。 With the rapid development of China's petrochemical industry, various waste oil residual liquids are inevitably generated in the production process. In a large-scale device for producing ethylene by cracking, high temperature tar is present in the cracking process, and a downstream related device generates various waste oil residual liquids in the polymerization process. These waste oil residual liquids have various physical and chemical properties, and include colloidal asphaltene, liquid polymers, aromatic ring compounds having an olefin group, and used catalyst powder and fine carbon granules. In addition, with the tightening of safety and environmental protection policies, if these waste oils cannot be used after being detoxified within the company, it will limit the sustainable development of the company.
したがって、さまざまな汚油残液を集中して処理する装置を提供することで、良好な経済的利益、環境的利益及び社会的利益を作り出すことは、当業者にとって解決しなければならない課題となっている。 Therefore, it is a problem to be solved by a person skilled in the art to create good economic, environmental and social benefits by providing a device for centrally treating various waste oil residual liquids. ing.
新しいタール残渣の処理方法及び装置であって、該装置は、タール残液混合撹拌タンク、タール残液供給タンク、加熱コイル、タール残液供給ポンプ、一次残液蒸発器、一次残液気液分離器ａ、一次残液気液分離器、排気凝縮器、酢酸貯蔵タンク、二次残液蒸発器、二次残液凝縮器、タール残渣収集タンク、精留酢酸精製塔を備える。 A new method and apparatus for treating tar residue, which comprises a tar residual liquid mixing and stirring tank, a tar residual liquid supply tank, a heating coil, a tar residual liquid supply pump, a primary residual liquid evaporator, and a primary residual liquid-gas separation. It is equipped with a vessel a, a primary residual liquid gas-liquid separator, an exhaust condenser, an acetic acid storage tank, a secondary residual liquid evaporator, a secondary residual liquid condenser, a tar residue collection tank, and a rectification acetic acid purification column.
以上を踏まえて、本発明は、化学工業における汚油残液の高効率浄化処理用の分離装置及び方法を提供し、これら汚油残液を集中して回収し効率よく浄化処理することを目的とする。 Based on the above, the present invention provides a separation device and method for highly efficient purification treatment of waste oil residual liquid in the chemical industry, and an object of the present invention is to collect these waste oil residual liquid in a concentrated manner for efficient purification treatment. And
上記目的を達成するために、本発明は、下記技術案を採用する。 In order to achieve the above object, the present invention adopts the following technical solutions.
本発明の第１態様の実施例は、化学工業から排出される廃油・廃液の高効率浄化処理用の分離装置を提供し、該装置は、貯蔵設備、蒸留分離設備、静的混合設備、重力沈降設備を備え、その中で、
前記貯蔵設備は、軽質易揮発性汚油残液を貯蔵するための球形タンク（Ｃ１）と、重質難揮発性汚油残液を貯蔵するための普通貯蔵タンク（Ｃ２）とを備え、前記球形タンク（Ｃ１）には、清澄液を排出するための第１排出口が設けられ、前記普通貯蔵タンク（Ｃ２）には、清澄液を排出するための第２排出口が設けられ、前記第１排出口は、第１ポンプ（Ｐ１）を介して第１熱交換器（Ｅ１）の入り口側に接続され、前記第２排出口は、第２ポンプ（Ｐ２）を介して前記第１熱交換器（Ｅ１）の入り口側に接続され、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）が前記第１熱交換器（Ｅ１）に接続される共通管路には、第１バルブ（Ｖ１）が設けられ、
前記蒸留分離設備は、精留塔（Ｔ１）を備え、前記精留塔（Ｔ１）の内部には、塔頂に位置する塔頂気相排出口、塔外周面に位置する清澄液供給口及び塔底に位置する塔底液相排出口が設けられ、前記第１熱交換器（Ｅ１）の出口側が第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して前記清澄液供給口に接続され、前記塔頂気相排出口は、前記第１熱交換器（Ｅ１）を介して還流タンク（Ｃ３）の入り口に接続され、前記精留塔（Ｔ１）には、塔頂還流口がさらに設けられ、前記還流タンク（Ｃ３）は、還流ポンプ（Ｐ３）を介して前記塔頂還流口に接続されて、塔頂の温度を調整して塔頂留出油に要求される品質を制御する液相還流を形成させ、
前記静的混合設備は、静的混合器（Ｍ１）を備え、前記静的混合器（Ｍ１）には、油類入り口、洗浄水入り口及び油水混合物出口が設けられ、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）は、また同一管路を介して該油類入り口に接続され、該同一管路には、第２バルブ（Ｖ２）が設けられ、前記還流タンク（Ｃ３）は、管路を介して該油類入り口に接続され、還流タンク（Ｃ３）と該油類入り口との間には、第３バルブ（Ｖ３）が設けられ、
前記重力沈降設備は、重力沈降タンク（Ｃ４）を備え、前記重力沈降タンク（Ｃ４）には、タンク上面に位置する気相排出口及び油水混合物入り口、タンク下面に位置する清澄液を排出するための第３排出口及び油含有汚水排出口が設けられ、前記油水混合物入り口は、管路を介して前記油水混合物出口に接続され、前記第３排出口は、順次第５ポンプ（Ｐ５）、第４バルブ（Ｖ４）を介して前記第１熱交換器（Ｅ１）に接続され、前記第４バルブ（Ｖ４）に接続されていない前記第５ポンプ（Ｐ５）の管路には、第５バルブ（Ｖ５）が設けられ、前記塔頂気相排出口は、管路を介して前記第５バルブ（Ｖ５）の出口に接続され、前記塔頂気相排出口と前記第５バルブ（Ｖ５）の出口との間の管路には、第６バルブ（Ｖ６）が設けられる。
The embodiment of the first aspect of the present invention provides a separation device for highly efficient purification treatment of waste oil/liquid discharged from the chemical industry, which comprises a storage facility, a distillation separation facility, a static mixing facility, a gravity facility. Equipped with settling equipment, in which
The storage facility is provided with a spherical-shaped tank for storing a light volatile dirty oil residual liquid (C1), and a common storage tank for storing the heavy flame volatile dirty oil residual liquid (C2), the front Symbol sphere shape tank (C1), a first outlet for discharging the clarified liquid is provided, wherein the common storage tank (C2), a second outlet for discharging the clarified liquid is provided , The first outlet is connected to the inlet side of the first heat exchanger (E1) via a first pump (P1), and the second outlet is connected to the first side via a second pump (P2). The first pipe is connected to the inlet side of the first heat exchanger (E1), and the first pump (P1) and the second pump (P2) are connected to the first heat exchanger (E1). A valve (V1) is provided,
The distillation separation equipment includes a rectification column (T1), and inside the rectification column (T1), a top gas phase outlet located at the top of the column, a clear liquid supply port located on the outer peripheral surface of the column, and A bottom liquid phase outlet located at the bottom of the tower is provided, and the outlet side of the first heat exchanger (E1) passes through the second heat exchanger (E2) and the third heat exchanger (E3) to obtain the clarified liquid. The top gas phase outlet is connected to the inlet, and is connected to the inlet of the reflux tank (C3) through the first heat exchanger (E1). A reflux port is further provided, and the reflux tank (C3) is connected to the overhead reflux port via a reflux pump (P3) to adjust the temperature at the top of the column and is required for overhead distillate oil. Form a liquid phase reflux that controls the quality,
The static mixing equipment comprises a static mixer (M1), the static mixer (M1) is provided with an oil inlet, a wash water inlet and an oil/water mixture outlet, and the first pump (P1). , The second pump (P2) is also connected to the oil inlet through the same pipeline, a second valve (V2) is provided in the same pipeline, and the reflux tank (C3) is a pipe. A third valve (V3) is provided between the reflux tank (C3) and the oil inlet, which is connected to the oil inlet through a passage.
The gravity settling equipment includes a gravity settling tank (C4), and the gravity settling tank (C4) discharges a gas phase discharge port and an oil/water mixture inlet located on the upper surface of the tank, and a clearing liquid located on the lower surface of the tank. A third outlet and an oil-containing wastewater outlet are provided, the oil-water mixture inlet is connected to the oil-water mixture outlet through a pipe, and the third outlet is sequentially connected to a fifth pump (P5), A fifth valve (P5) is connected to the first heat exchanger (E1) through a four valve (V4) and is not connected to the fourth valve (V4). V5) is provided, and the top gas phase discharge port is connected to the outlet of the fifth valve (V5) via a pipeline, and the top gas phase discharge port and the outlet of the fifth valve (V5) are provided. A sixth valve (V6) is provided in the conduit between and.
本発明の第１態様の実現可能な形態によれば、前記精留塔（Ｔ１）は、精留部及びストリッピング部を備え、前記精留部には、高性能パッキング分離部材が使用され、ストリッピング部には、コーキング防止可能な大容量ランダムパッキングが使用される。 According to a feasible form of the first aspect of the present invention, the rectification column (T1) comprises a rectification section and a stripping section, and a high performance packing separation member is used in the rectification section, A large capacity random packing capable of preventing coking is used for the stripping section.
本発明の第１態様の実現可能な形態によれば、前記精留塔（Ｔ１）のボトムには、放散蒸気入り口（Ｓ１）がさらに設けられている。 According to a feasible form of the first aspect of the present invention, a desorption steam inlet (S1) is further provided at the bottom of the rectification column (T1).
本発明の第１態様の実現可能な形態によれば、前記第１バルブ（Ｖ１）と第３バルブ（Ｖ３）の間には、分岐バルブ（Ｖ７）が設けられ、前記分岐バルブ（Ｖ７）が開かれたとき、前記精留塔（Ｔ１）から蒸留された一部の低沸点炭化水素類物質が、前記分岐バルブ（Ｖ７）を介して前記第１バルブ（Ｖ１）からの清澄液と混合する。 According to the feasible mode of the first aspect of the present invention, a branch valve (V7) is provided between the first valve (V1) and the third valve (V3), and the branch valve (V7) is provided. When opened, some low boiling hydrocarbons substances distilled from the rectification column (T1) mix with the clarified liquid from the first valve (V1) via the branch valve (V7). ..
本発明の第２態様は、化学工業における汚油残液の高効率浄化処理用の方法を提供し、該方法は、前記装置を用い、処理対象となる化学工業における汚油残液の性質に応じて、蒸留−水洗及び水洗−蒸留、または蒸留−水洗・水洗−蒸留のどちらかの処理方法を実施する。 A second aspect of the present invention provides a method for highly efficient purification treatment of waste oil residual liquid in the chemical industry, which uses the above-mentioned apparatus to determine the property of the waste oil residual liquid in the chemical industry to be treated. Depending on the treatment method, either distillation-water washing and water-washing-distillation, or distillation-water washing/water-washing-distillation is carried out.
本発明の第２態様の実現可能な形態によれば、前記蒸留−水洗処理方法の手順は、以下のとおりである。
第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を開け、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を閉め、第１ポンプ（Ｐ１）を起動させて球形タンク（Ｃ１）における清澄液を吸い出すとともに、第２ポンプ（Ｐ２）を起動させて普通貯蔵タンク（Ｃ２）における清澄液を吸い出す。
生産の要求に対応する割合で球形タンク（Ｃ１）及び普通貯蔵タンク（Ｃ２）から吸い出された清澄液を混合し、順次第１熱交換器（Ｅ１）、第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して混合後の清澄液を精留塔（Ｔ１）に送り、前記精留塔（Ｔ１）で前記清澄液を蒸留処理し、発生させた低沸点炭化水素類物質及び水蒸気を凝縮させ、冷却させた後、還流タンク（Ｃ３）に送り、一部の低沸点炭化水素類物質を還流ポンプ（Ｐ３）で精留塔（Ｔ１）のトップに戻し、還流タンク（Ｃ３）からの低沸点炭化水素類物質を静的混合器（Ｍ１）に送る。
前記静的混合器（Ｍ１）に水を加えて、低沸点炭化水素類物質と水を所定の割合で静的混合器（Ｍ１）において混合して洗浄を行い、洗浄して得られた油水混合物を重力沈降タンク（Ｃ４）に送り、さらに重力沈降タンク（Ｃ４）による不均一相分離により水洗のステップを完了する。
According to the feasible mode of the second aspect of the present invention, the procedure of the distillation-water washing treatment method is as follows.
The first valve (V1), the third valve (V3) and the fifth valve (V5) are opened, the second valve (V2), the fourth valve (V4) and the sixth valve (V6) are closed, and the first pump ( P1) was allowed to start with sucking the clarified liquid in the sphere-shaped tank (C1), sucked out clarified liquid on plain storage tank (C2) activates the second pump (P2).
Clarified liquid that has been sucked out of the sphere-shaped tank (C1) and common storage tank (C2) at a rate corresponding to the request of producing mixed, order soon first heat exchanger (E1), a second heat exchanger (E2) , The low-boiling hydrocarbons generated by sending the mixed clarified liquid to the rectification column (T1) through the third heat exchanger (E3) and subjecting the clarified liquid to distillation treatment in the rectification column (T1). After condensing the similar substances and water vapor and cooling them, they are sent to a reflux tank (C3), and some low-boiling point hydrocarbon substances are returned to the top of the rectification column (T1) by a reflux pump (P3), and then the reflux tank. The low boiling hydrocarbons material from (C3) is sent to the static mixer (M1).
Water is added to the static mixer (M1), low-boiling hydrocarbon substances and water are mixed in a predetermined ratio in the static mixer (M1) for washing, and an oil-water mixture obtained by washing Is sent to the gravity settling tank (C4), and the step of washing with water is completed by the heterogeneous phase separation by the gravity settling tank (C4).
前記水洗−蒸留処理方法の手順は、以下のとおりである。
第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を閉め、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を開け、第１ポンプ（Ｐ１）を起動させて球形タンク（Ｃ１）における清澄液を吸い出すとともに、第２ポンプ（Ｐ２）を起動させて普通貯蔵タンク（Ｃ２）における清澄液を吸い出す。
生産の要求に対応する割合で球形タンク（Ｃ１）及び普通貯蔵タンク（Ｃ２）から吸い出された清澄液を混合し、混合後の清澄液を静的混合器（Ｍ１）に入れる。
前記静的混合器（Ｍ１）に水を加えて、前記混合後の清澄液と水を所定の割合で静的混合器（Ｍ１）において混合して洗浄を行い、洗浄して得られた油水混合物を重力沈降タンク（Ｃ４）に送り、さらに重力沈降タンク（Ｃ４）による不均一相分離により水洗のステップを完了し、順次第１熱交換器（Ｅ１）、第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して水洗後の清澄液を精留塔（Ｔ１）に送り、精留塔（Ｔ１）で蒸留処理し、低沸点炭化水素類物質と高沸点炭化水素類物質に分離させ、蒸留分離ステップを完了する。
The procedure of the water washing-distillation treatment method is as follows.
The first valve (V1), the third valve (V3) and the fifth valve (V5) are closed, the second valve (V2), the fourth valve (V4) and the sixth valve (V6) are opened, and the first pump ( P1) was allowed to start with sucking the clarified liquid in the sphere-shaped tank (C1), sucked out clarified liquid on plain storage tank (C2) activates the second pump (P2).
Clarified liquid that has been sucked out of the sphere-shaped tank (C1) and common storage tank (C2) at a rate corresponding to the requirements of production were mixed, put it clarified liquid after mixing in a static mixer (M1).
Water is added to the static mixer (M1), and the clarified liquid after mixing and water are mixed in a predetermined ratio in the static mixer (M1) for washing, and an oil-water mixture obtained by washing To the gravity settling tank (C4), and the step of washing with water is completed by the non-uniform phase separation by the gravity settling tank (C4), and the first heat exchanger (E1), the second heat exchanger (E2) and the The clarified liquid after washing with water is sent to the rectification column (T1) through the 3 heat exchanger (E3) and subjected to distillation treatment in the rectification column (T1) to obtain low boiling point hydrocarbon substances and high boiling point hydrocarbon substances. Separate and complete the distillation separation step.
本発明の第２態様の実現可能な形態によれば、前記球形タンク（Ｃ１）の操作温度は、１〜７０℃、普通貯蔵タンク（Ｃ２）の操作温度は、１〜１００℃、球形タンク（Ｃ１）、普通貯蔵タンク（Ｃ２）の操作圧力は、いずれも０〜０．８ＭＰａであり、
前記精留塔（Ｔ１）では、操作温度が常温４０〜３００℃、操作圧力が０〜０．５ＭＰａであり、
前記静的混合器（Ｍ１）では、操作温度が２〜８０℃、操作圧力が０〜０．８ＭＰａであり、
前記重力沈降タンク（Ｃ４）では、操作温度が２〜８０℃、操作圧力が０〜０．５ＭＰａであり、
前記還流タンク（Ｃ３）では、操作温度が２〜６０℃、操作圧力が０〜０．５ＭＰａである。
According to a second aspect of the feasible embodiment of the present invention, the operating temperature of the pre-Symbol sphere shape tank (C1) is, 1 to 70 ° C., the operating temperature of common storage tank (C2) is, 1 to 100 ° C., spheres The operating pressure of the shaped tank (C1) and the ordinary storage tank (C2) are both 0 to 0.8 MPa,
In the rectification column (T1), the operating temperature is room temperature 40 to 300° C., the operating pressure is 0 to 0.5 MPa,
In the static mixer (M1), the operating temperature is 2 to 80° C., the operating pressure is 0 to 0.8 MPa,
In the gravity settling tank (C4), the operating temperature is 2 to 80° C., the operating pressure is 0 to 0.5 MPa,
In the reflux tank (C3), the operating temperature is 2 to 60°C and the operating pressure is 0 to 0.5 MPa.
上記技術案から分かるように、従来技術に比べて、本発明の有益な効果は、以下のとおりである。
１．エチレンプラントの各操作ユニット由来の汚油残液を易揮発性、難揮発性の２つの種類に分けて、それぞれ球形タンク（Ｃ１）及び普通貯蔵タンク（Ｃ２）に供給し、それによって、すべての汚油残液が球形タンク（Ｃ１）に供給されることを回避することができる。その後、集中して効率よく浄化処理を行う。
２．清澄液の性質に応じて操作プロセスを切り替えることにより、汚油残液における高品質成分を十分に利用し、汚油残液の利用率を向上させて、環境汚染を低減させる。
３．精留塔（Ｔ１）を分離装置として、塔底から水蒸気を吹き込んで油蒸気の分圧を低下させ、塔底の温度を低下させることによって、占有する面積を減少させて、設備投資を低下させ、塔底油の熱重縮合を減少させ、また、塔底の熱量を統合することでエネルギーの利用を最大化させる。
４．化学工業における汚油残液は、集中回収され、効率よく浄化処理されて、その中で下流加工装置により求められる原料性質を満たす回収塔頂留分油の割合は５０％〜８０％である。塔底釜液と沈降液をブレンドすると、遅延コーキング装置により求められる原料の性質を満たし、又は舶舶用残渣燃料油の性質への要件を満たす。
５．プロセスの柔軟性が高く、即ち、蒸留−水洗の形態も水洗−蒸留の形態も利用可能であり、分岐バルブを設けることにより、廃油原料性質の多様性に対応でき、超重質・超高粘度の汚油残液原料の処理に適用できる。
As can be seen from the above technical solution, the beneficial effects of the present invention are as follows, compared with the prior art.
1. Volatile the dirty oil residual liquid from each operating unit of an ethylene plant, in two kinds of sparingly volatile, supplied to their respective ball-shaped tank (C1) and common storage tank (C2), whereby , it is possible to avoid that all dirty oil residual liquid is supplied to the spherical-shaped tank (C1). After that, the treatment is concentrated and efficiently performed.
2. By switching the operation process depending on the properties of the clarified liquid, the high-quality components in the sewage residual liquid are fully utilized, the utilization ratio of the sewage residual liquid is improved, and environmental pollution is reduced.
3. The rectification tower (T1) is used as a separation device to inject steam from the bottom of the tower to lower the partial pressure of the oil vapor and lower the temperature of the bottom of the tower, thereby reducing the occupied area and lowering the capital investment. , Reduce the thermal polycondensation of bottom oil and maximize the utilization of energy by integrating the heat quantity of the bottom oil.
4. The waste oil residual liquid in the chemical industry is intensively collected and efficiently purified, and the ratio of the recovered overhead fraction oil satisfying the raw material properties required by the downstream processing device is 50% to 80%. When the bottom kettle liquid and the sediment are blended, the properties of the raw material required by the delayed coking device are satisfied, or the properties of the residual fuel oil for ships and vessels are satisfied.
5. The process flexibility is high, that is, both the distillation-water washing mode and the water-washing-distillation mode can be used.By providing a branch valve, it is possible to cope with a variety of waste oil raw material properties, and to achieve ultra-heavy/ultra-high viscosity. It can be applied to the treatment of raw material for residual oil from dirty oil.
本発明の実施例又は従来技術における技術案をより明瞭に説明するために、以下、実施例又は従来技術の説明に必要な図面を簡単に説明するが、明らかなように、以下の説明における図面は、本発明の実施例に過ぎず、当業者であれば、創造的な努力を必要とせずに、これら図面に基づいてほかの図面を取得できる。 In order to more clearly describe the technical solutions in the embodiments of the present invention or the prior art, the drawings necessary for explaining the embodiments or the prior art will be briefly described below, but as is apparent, the drawings in the following description Are merely embodiments of the present invention, and those skilled in the art can obtain other drawings based on these drawings without creative efforts.
以下、本発明の実施例における技術案を明瞭で完全に説明するが、明らかなように、説明される実施例は、本発明の実施例の一部に過ぎず、すべての実施例ではない。当業者であれば、本発明の実施例に基づいて創造的な努力を必要とせずに取得し得るほかの実施例は、すべて本発明の特許範囲に属する。 Hereinafter, the technical solutions in the embodiments of the present invention will be described clearly and completely, but as is apparent, the embodiments described are only a part of the embodiments of the present invention and not all the embodiments. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the patent scope of the present invention.
図１を参照しながら本発明をさらに説明すると、本発明は、化学工業における汚油残液の高効率浄化処理用の装置及び方法を提供し、本装置は、貯蔵設備、蒸留分離設備、静的混合設備、重力沈降設備を備える。 The present invention will be further described with reference to FIG. 1. The present invention provides an apparatus and method for highly efficient purification treatment of waste oil residual liquid in the chemical industry, which comprises a storage facility, a distillation separation facility, and a static separation facility. Equipped with static mixing equipment and gravity settling equipment.
前記貯蔵設備は、軽質易揮発性汚油残液を貯蔵するための球形タンク（Ｃ１）と、重質難揮発性汚油残液を貯蔵するための普通貯蔵タンク（Ｃ２）とを備え、前記球形タンク（Ｃ１）には、清澄液を排出するための第１排出口が設けられ、前記普通貯蔵タンク（Ｃ２）には、清澄液を排出するための第２排出口が設けられ、前記第１排出口は、第１ポンプ（Ｐ１）を介して第１熱交換器（Ｅ１）の入り口側に接続され、前記第２排出口は、第２ポンプ（Ｐ２）を介して前記第１熱交換器（Ｅ１）の入り口側に接続され、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）が前記第１熱交換器（Ｅ１）に接続される共通管路には、第１バルブ（Ｖ１）が設けられ、
前記蒸留分離設備は、精留塔（Ｔ１）を備え、前記精留塔（Ｔ１）の内部には、上から下へ順次塔頂気相排出口、清澄液供給口及び塔底液相排出口が設けられ、前記第１熱交換器（Ｅ１）の出口側が第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して前記清澄液供給口に接続され、前記塔頂気相排出口は、前記第１熱交換器（Ｅ１）を介して還流タンク（Ｃ３）の入り口に接続され、前記精留塔（Ｔ１）には、塔頂還流口がさらに設けられ、前記還流タンク（Ｃ３）は、還流ポンプ（Ｐ３）を介して前記塔頂還流口に接続されて、塔頂の温度を調整して塔頂留出油に要求される品質を制御する液相還流を形成させ、
前記静的混合設備は、静的混合器（Ｍ１）を備え、前記静的混合器（Ｍ１）には、油類入り口、洗浄水入り口及び油水混合物出口が設けられ、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）は、また同一管路を介して該油類入り口に接続され、該同一管路には、第２バルブ（Ｖ２）が設けられ、前記還流タンク（Ｃ３）は、管路を介して該油類入り口に接続され、還流タンク（Ｃ３）と該油類入り口との間には、第３バルブ（Ｖ３）が設けられ、
前記重力沈降設備は、重力沈降タンク（Ｃ４）を備え、前記重力沈降タンク（Ｃ４）には、上から下へ順次気相排出口、油水混合物入り口、清澄液を排出するための第３排出口、油含有汚水排出口が設けられ、前記油水混合物入り口は、管路を介して前記油水混合物出口に接続され、前記第３排出口は、順次第５ポンプ（Ｐ５）、第４バルブ（Ｖ４）を介して前記第１熱交換器（Ｅ１）に接続され、前記第４バルブ（Ｖ４）に接続されていない前記第５ポンプ（Ｐ５）の管路には、第５バルブ（Ｖ５）が設けられ、前記塔頂気相排出口は、管路を介して前記第５バルブ（Ｖ５）の出口に接続され、前記塔頂気相排出口と前記第５バルブ（Ｖ５）の出口との間の管路には、第６バルブ（Ｖ６）が設けられる。
The storage facility is provided with a spherical-shaped tank for storing a light volatile dirty oil residual liquid (C1), and a common storage tank for storing the heavy flame volatile dirty oil residual liquid (C2), the front Symbol sphere shape tank (C1), a first outlet for discharging the clarified liquid is provided, wherein the common storage tank (C2), a second outlet for discharging the clarified liquid is provided , The first outlet is connected to the inlet side of the first heat exchanger (E1) via a first pump (P1), and the second outlet is connected to the first side via a second pump (P2). The first pipe is connected to the inlet side of the first heat exchanger (E1), and the first pump (P1) and the second pump (P2) are connected to the first heat exchanger (E1). A valve (V1) is provided,
The distillation separation equipment comprises a rectification tower (T1), and inside the rectification tower (T1), from top to bottom, a top gas phase outlet, a clarified liquid supply inlet, and a bottom liquid phase outlet. Is provided, the outlet side of the first heat exchanger (E1) is connected to the fining liquid supply port through the second heat exchanger (E2) and the third heat exchanger (E3), and the top gas phase The discharge port is connected to the inlet of the reflux tank (C3) through the first heat exchanger (E1), and the rectification column (T1) is further provided with an overhead reflux port, and the reflux tank ( C3) is connected to the overhead reflux port via a reflux pump (P3) to form a liquid phase reflux for adjusting the temperature at the overhead to control the quality required for overhead distillate,
The static mixing equipment comprises a static mixer (M1), the static mixer (M1) is provided with an oil inlet, a wash water inlet and an oil/water mixture outlet, and the first pump (P1). , The second pump (P2) is also connected to the oil inlet through the same pipeline, a second valve (V2) is provided in the same pipeline, and the reflux tank (C3) is a pipe. A third valve (V3) is provided between the reflux tank (C3) and the oil inlet, which is connected to the oil inlet through a passage.
The gravity settling equipment is provided with a gravity settling tank (C4), and the gravity settling tank (C4) is provided with a gas phase discharge port, an oil/water mixture inlet port, and a third discharge port for discharging a clear liquid in order from top to bottom. An oil-containing sewage outlet is provided, the oil-water mixture inlet is connected to the oil-water mixture outlet through a pipe, and the third outlet is sequentially connected to a fifth pump (P5) and a fourth valve (V4). A fifth valve (V5) is provided in a pipe line of the fifth pump (P5) which is connected to the first heat exchanger (E1) via the and which is not connected to the fourth valve (V4). The overhead gas phase outlet is connected to an outlet of the fifth valve (V5) via a pipe line, and a pipe between the overhead gas phase outlet and the outlet of the fifth valve (V5). A sixth valve (V6) is provided in the passage.
１つの実現可能な形態では、前記精留塔（Ｔ１）は、精留部及びストリッピング部を備え、精留部には、高性能パッキング分離部材（３−２０段の理論段に相当）が使用され、ストリッピング部には、コーキング防止可能な大容量ランダムパッキング（１−３段の理論段に相当）が使用され、供給段は気液を供給してフラッシュ蒸発を行う空間（１段の理論段に相当）であり、塔頂には、塔頂の温度を調整して塔頂留出油に要求される品質を制御するための液相還流が設けられる。１つの実現可能な形態では、前記精留塔（Ｔ１）のボトムには、放散蒸気入り口（Ｓ１）がさらに設けられており、熱量を供給して気相還流を発生させるためにリボイラーが塔底に設けられるのではなく、塔底の液面の上方へ水蒸気を直接吹き込んで放散を行い、それにより、油蒸気の分圧を低下させて、ストリッピング作用を高めるという効果を奏する。 In one feasible form, the rectification column (T1) comprises a rectification part and a stripping part, the rectification part being provided with a high performance packing separation member (corresponding to 3-20 theoretical plates). Used in the stripping section, large-capacity random packing capable of preventing coking (corresponding to 1 to 3 theoretical stages) is used, and the supply stage supplies a space for flash vaporization by supplying gas-liquid (one stage). It corresponds to the theoretical plate), and the top of the column is provided with a liquid phase reflux for adjusting the temperature at the top of the column to control the quality required of the overhead distillate oil. In one feasible form, the bottom of the rectification column (T1 ) is further provided with a desorption steam inlet (S1) and a reboiler is installed at the bottom of the column to supply heat and generate gas phase reflux. Instead of being installed in the column, steam is blown directly above the liquid surface at the bottom of the column to diffuse the vapor, thereby reducing the partial pressure of the oil vapor and enhancing the stripping action.
１つの実現可能な形態では、前記第１バルブ（Ｖ１）と第３バルブ（Ｖ３）との間には、分岐バルブ（Ｖ７）が設けられ、前記分岐バルブ（Ｖ７）が開かれたとき、分岐バルブ（Ｖ７）を通った一部の低沸点炭化水素類物質は第１バルブ（Ｖ１）の方向へ進んで、第１熱交換器（Ｅ１）の上部の位置で第１バルブ（Ｖ１）からの清澄液と混合し、混合後に第１熱交換器（Ｅ１）を通って第２熱交換器（Ｅ２）へ向かう。汚油残液の性質を、装置に入る前に調整することはできないが、分岐バルブ（Ｖ７）及び対応する操作によって可能になり、このため、極めて重くて（標準密度≦１０５０ｋｇ／ｍ３）粘度が高い（５０℃動粘度≦２００ｍｍ２／ｓ）汚油残液を処理して分離することができ、分離装置及び方法の汎用性を向上させることができる。 In one possible embodiment, the first valve (V1) between the third valve (V3), the branch valve (V7) is provided, wherein when the branch valve (V7) is opened, the branch A part of the low boiling point hydrocarbon substances passing through the valve (V7) proceeds toward the first valve (V1) and is discharged from the first valve (V1) at a position above the first heat exchanger (E1). After mixing with the clarified liquid, it goes through the first heat exchanger (E1) to the second heat exchanger (E2) after mixing. The properties of the residual oil residue cannot be adjusted before entering the device, but are made possible by the branch valve (V7) and the corresponding operation, which makes it extremely heavy (standard density ≤ 1050 kg/m 3 ) viscosity. It is possible to treat and separate a dirty oil residual liquid having a high viscosity (kinematic viscosity at 50° C.≦200 mm 2 /s) and improve the versatility of the separating apparatus and method.
本発明に係る化学工業における汚油残液の高効率浄化処理用の方法は、上記装置を用い、回収された汚油残液原料の性質に応じて、蒸留−水洗（スキーム１）又は水洗−蒸留（スキーム２）の２種の異なる技術手段に従って浄化分離処理を効率よく実施できる。 The method for highly efficient purification treatment of waste oil residual liquor in the chemical industry according to the present invention uses the above-mentioned apparatus, and depending on the properties of the recovered waste oil residual liquor raw material, distillation-water washing (Scheme 1) or water washing- The purification separation process can be efficiently carried out according to two different technical means of distillation (Scheme 2).
清澄液の品質が高い場合、スキーム１に従って操作を行い（第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を開け、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を閉める）、球形タンク（Ｃ１）からの軽質汚油残液（Ｆ１）と普通貯蔵タンク（Ｃ２）からの重質汚油残液（Ｆ２）とを生産の要求に従って管路において混合し、第１バルブ（Ｖ１）を通過させて、順次塔頂留分油（Ｄ）、塔底重質油（Ｒ）と熱交換させ、最後に、中圧蒸気と熱交換させて、精留塔（Ｔ１）に入れて分離させる。放散蒸気は、制御バルブを操作することにより精留塔の塔底の液面の上方に至り、塔底へ流れる液相流れを放散させ、それにおける軽質成分をストリッピングする。精留塔（Ｔ１）では、操作温度が４０〜３００℃、操作圧力が０．１〜０．５ＭＰａ、塔全体の理論段数が５〜２４段である。低沸点の軽質成分及び水蒸気は、下から上へと塔頂に流れて、熱交換器、水冷器を通過した後、操作温度２〜６０℃、操作圧力０．１〜０．５ＭＰａの還流タンク（Ｃ３）に入る。それにおける気相物質は、気体炭化水素（Ｇ）としてガスパイプラインに入り、油含有汚水は、汚水処理装置に排出され、液相の塔頂留分油（Ｄ）は、一部が塔頂冷還流として塔頂の温度を制御し、塔頂留分油（Ｄ）の乾燥ポイントを確保し、過剰な部分が塔頂留分油として水洗ユニットに送られる。蒸留により得られた塔頂留分油（Ｄ）は、第３バルブ（Ｖ３）を通過した後、一定の割合の新しい水（油と水の質量比は３：１）に同伴して、操作温度２〜８０℃、操作圧力０．１〜０．８ＭＰａの静的混合器（Ｍ１）に入り強力に混合され、強力に混合されると、油における水に可溶な塩類、非炭化水素類化合物を溶解させることができ、次に、操作温度２〜８０℃、操作圧力０．１〜０．５ＭＰａの重力沈降タンク（Ｃ４）に送り油水分離を行う。重力沈降タンク（Ｃ４）のボトムの水ドラムにおける洗浄廃水と還流タンク（Ｃ３）における油含有汚水は、一緒に汚水処理装置に送られ、洗浄された留分油は、下流の水素化装置の原料タンクに入り、水素化精製原料油として高品質の油製品に変換される。 When the quality of the clarified liquid is high, operation is performed according to scheme 1 (first valve (V1), third valve (V3), fifth valve (V5) is opened, second valve (V2), fourth valve (V4) ), sixth closing valve (V6)), from spherical-shaped tank (C1) light fouling oil residual liquid (F1) and ordinary storage heavy fouling oil bottoms from the tank (C2) (F2) and the production According to the requirements, they are mixed in a pipe, passed through a first valve (V 1 ), and are sequentially heat-exchanged with a top distillate oil (D) and a bottom heavy oil (R), and finally, with medium pressure steam. It heat-exchanges and it puts in a rectification tower (T1), and is separated. The desorbed vapor reaches the upper side of the liquid level at the bottom of the rectification column by operating the control valve, disperses the liquid phase flow flowing to the column bottom, and strips the light components therein. In the rectification column (T1), the operating temperature is 40 to 300° C., the operating pressure is 0.1 to 0.5 MPa, and the total number of theoretical plates is 5 to 24. The low-boiling light components and water vapor flow from the bottom to the top of the tower, and after passing through a heat exchanger and a water cooler, a reflux tank having an operating temperature of 2 to 60° C. and an operating pressure of 0.1 to 0.5 MPa. Enter (C3). The gas phase substances therein enter the gas pipeline as gaseous hydrocarbons (G), the oil-containing wastewater is discharged to the wastewater treatment equipment, and the liquid phase overhead distillate (D) is partially cooled overhead. The temperature at the top of the tower is controlled as reflux, a drying point of the overhead fraction oil (D) is secured, and the excess portion is sent to the water washing unit as the overhead fraction oil. By distillation resulting top distillate oil (D) passes through the third valve (V 3), (the weight ratio of oil and water 3: 1) fresh water of a certain percentage by entrained, When the mixture is vigorously mixed into a static mixer (M1) having an operating temperature of 2 to 80° C. and an operating pressure of 0.1 to 0.8 MPa, when it is vigorously mixed, water-soluble salts and non-hydrocarbons in oil The similar compound can be dissolved, and then the oil-water separation is carried out to a gravity settling tank (C4) having an operating temperature of 2 to 80° C. and an operating pressure of 0.1 to 0.5 MPa. The washing wastewater in the bottom water drum of the gravity settling tank (C4) and the oil-containing wastewater in the reflux tank (C3) are sent together to the wastewater treatment device, and the washed distillate oil is the raw material of the downstream hydrogenation device. It enters the tank and is converted into high-quality oil products as hydrorefined feedstock.
実施例Ａ
清澄液の品質が低い場合、スキーム２に従って操作を行い（第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を閉め、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を開ける）、球形タンク（Ｃ１）からの軽質汚油残液（Ｆ１）と普通貯蔵タンク（Ｃ２）からの重質汚油残液（Ｆ２）を生産の要求に従って管路において混合させ、第２バルブ（Ｖ２）を通過させて、一定の割合の新しい水（油と水の質量比は４：１）に同伴して静的混合器（Ｍ１）に入れて、強力に混合させた後、重力沈降タンク（Ｃ４）に送り、油水分離を行う。静的混合器（Ｍ１）では、操作温度が２〜８０℃、操作圧力が０．１〜０．８ＭＰａである。強力に混合した後、油における水に可溶な塩類、非炭化水素類混合物を溶解させることができ、次に、管路を介して油水混合物を、操作温度２〜８０℃、操作圧力０．１〜０．５ＭＰａの重力沈降タンク（Ｃ４）に入れて、洗浄沈降操作により不均一相分離を行い、それによって気体炭化水素（Ｇ）は、タンクのトップから抜き出され、管路、制御バルブを介してガスパイプラインに導入され、洗浄水は、タンクの底部の水ドラムから汚水処理装置に排出され、洗浄後の清澄液は、タンクのボトムから抜き出され、管路、第４バルブ（Ｖ４）を通過した後、順次塔頂留分油（Ｄ）、塔底重質油（Ｒ）と熱交換し、最後に中圧蒸気と熱交換し、精留塔（Ｔ１）に入って分離される。放散蒸気は、制御バルブを操作することにより精留塔（Ｔ１）の塔底の液面の上方に送られ、塔底へ流れる液相物流を放散させて、それにおける軽質成分をストリッピングする。精留塔（Ｔ１）では、操作温度が４０〜３００℃、操作圧力が０．１〜０．５ＭＰａ、塔全体の理論段数が５〜２４段である。低沸点の軽質成分及び水蒸気は、下から上へと塔頂に流れて、熱交換器、水冷器を通過した後、操作温度２〜６０℃、操作圧力０．１〜０．５ＭＰａの還流タンク（Ｃ３）に送られる。それにおける気相物質は、気体炭化水素（Ｇ）としてガスパイプラインに入り、油含有汚水は、重力沈降タンク（Ｃ４）の洗浄水とともに汚水処理装置に排出され、液相の塔頂留分油（Ｄ）は、一部が塔頂冷還流として塔頂の温度を制御し、塔頂留分油（Ｄ）の乾燥ポイントを確保し、過剰な部分が塔頂留分油として下流の水素化装置の原料タンクに送られ、水素化精製原料油として高品質の油製品に変換される。
Example A
When the quality of the clarified liquid is low, operation is performed according to Scheme 2 (first valve (V1), third valve (V3), fifth valve (V5) are closed, second valve (V2), fourth valve (V4) ), the sixth opening valves (V6)), a request producing heavy fouling oil residual liquid (F2) from the light-fouling oil from spherical-shaped tank (C1) bottoms (F1) and ordinary storage tank (C2) According to the method described above, mixed in a pipeline according to the method described above, passed through a second valve (V 2 ), and entrained in a static water mixer (oil/water mass ratio 4:1) in a static mixer (M1). After vigorously mixing, the mixture is sent to a gravity settling tank (C4) for oil-water separation. In the static mixer (M1), the operating temperature is 2 to 80°C and the operating pressure is 0.1 to 0.8 MPa. After vigorous mixing, the water-soluble salts in oil, a mixture of non-hydrocarbons, can be dissolved, and then the oil-water mixture is passed via a line at an operating temperature of 2-80° C. and an operating pressure of 0. It is put in a gravity sedimentation tank (C4) of 1 to 0.5 MPa, and heterogeneous phase separation is carried out by a washing sedimentation operation, whereby gaseous hydrocarbon (G) is extracted from the top of the tank, a pipeline, a control valve. The washing water is introduced into the gas pipeline through the tank, the washing water is discharged from the water drum at the bottom of the tank to the sewage treatment apparatus, and the clarified liquid after washing is taken out from the bottom of the tank, and the pipe line, the fourth valve (V After passing 4 ), heat is exchanged with the overhead distillate (D) and the bottom heavy oil (R) in sequence, and finally with medium pressure steam, and then enters the rectification column (T1) for separation. To be done. The desorbed vapor is sent to above the liquid level at the bottom of the rectification column (T1) by operating the control valve, and disperses the liquid phase stream flowing to the column bottom to strip light components therein. In the rectification column (T1), the operating temperature is 40 to 300° C., the operating pressure is 0.1 to 0.5 MPa, and the total number of theoretical plates is 5 to 24. The low-boiling light components and water vapor flow from the bottom to the top of the tower, and after passing through a heat exchanger and a water cooler, a reflux tank having an operating temperature of 2 to 60° C. and an operating pressure of 0.1 to 0.5 MPa. It is sent to (C3). The gas phase substance therein enters the gas pipeline as a gaseous hydrocarbon (G), and the oil-containing wastewater is discharged to the wastewater treatment equipment together with the wash water of the gravity settling tank (C4), and the liquid phase overhead fraction oil ( Part D) controls the temperature at the top of the tower as a cold reflux at the top to secure a drying point for the overhead fractionated oil (D), and an excess portion as the overhead fractionated oil as a downstream hydrogenation device. It is sent to the raw material tank of and is converted into high-quality oil products as hydrorefined raw material oil.
実施例１
化学工業における汚油残液の高効率浄化処理用の装置については、処理能力が２ｔ／ｈであり、本例では、１５種類の廃油を供給混合原料とし、その中で、６種類の汚油残液は、低沸点軽質成分（標準密度８００ｋｇ／ｍ３未満）であり、６５質量％を占め、９種類の汚油残液は、高沸点重質成分（標準密度８００ｋｇ／ｍ３超）であり、３５質量％を占めており、蒸留−水洗プロセスを用い、具体的な操作は、以下のとおりである。
球形タンク（Ｃ１）では、操作温度が２５℃、操作圧力が０．３５ＭＰａであり、普通貯蔵タンク（Ｃ２）では、操作温度が２５℃、操作圧力が０ＭＰａである。流出流れの質量流量については、球形タンク（Ｃ１）では、６５％、普通貯蔵タンク（Ｃ２）では、３５％であるように制御しながら、管路において常温で混合する。
精留塔（Ｔ１）の精留部は、２段規則パッキング（理論段数１２段）であり、ストリッピング部は、１段ランダムパッキング（理論段数３段）であり、汚油残液供給位置は、上から第２段と第３段のパッキングの間にあり、放散蒸気供給位置は、塔底の液面の上方（第３段パッキングの下部）にあり、塔頂からは、低沸点の留分油（即ち低沸点炭化水素類物質）及び水蒸気、塔底からは、高沸点重質油（即ち高沸点炭化水素類物質）が流出する。塔頂の還流比は０．７であり、塔底から吹き込まれる水蒸気は、塔底の重質油の５％（質量）であり、油蒸気の分圧を低下させて塔底温度を低下させる。塔底の操作温度が２２５℃、塔頂の操作温度が１１３℃、操作圧力が０．１３ＭＰａである。還流タンク（Ｃ３）では、操作温度が４０℃、操作圧力が０．１ＭＰａである。
蒸留により得られた留分油は、静的混合器（Ｍ１）に送られる。静的混合器（Ｍ１）に入った油と新しい常温水との質量比は、４：１であり、静的混合器（Ｍ１）では、操作温度が３７〜３８℃、操作圧力が０．６ＭＰａである。
重力沈降タンク（Ｃ４）では、操作温度が３７℃、操作圧力が０．２５ＭＰａである。
塔頂の熱い材料も塔底の熱い材料も新しい原料と熱交換し、熱統合を行い、それにより、できるだけ熱量を回収して、冷却水の使用量を低減させる。
上記条件によれば、回収可能な留分油の収率は、６３．１２％に達し、下流のガソリン水素化装置により求められる原料の性質を満たす。塔底重質油及び沈降液をブレンドすると、遅延コーキング装置により求められる原料の性質を満たし、又は舶残渣燃料油の性質を満たす。
実施例１に必要な汚油残液は、比較的クリーンであり、得られた水洗留分油は、それ以上クリーンであり、水洗水の使用量低減に有利であり、さらに水洗には、乳化現象が発生しない。
Example 1
An apparatus for highly efficient purification treatment of residual sewage oil in the chemical industry has a processing capacity of 2 t/h, and in this example, 15 kinds of waste oil are used as a feed mixed material, and 6 kinds of sewage oil are included in the mixture. The residual liquid is a low-boiling light component (standard density of less than 800 kg/m 3 ) and accounts for 65% by mass. The 9 types of waste oil residual liquid are high-boiling heavy components (standard density of over 800 kg/m 3 ). Yes, occupies 35% by mass, and uses a distillation-water washing process, and the specific operation is as follows.
In spherical-shaped tank (C1), operating temperature of 25 ° C., the operating pressure is 0.35 MPa, the ordinary storage tank (C2), operating temperature of 25 ° C., the operation pressure is 0 MPa. The mass flow rate of the effluent stream, the sphere-shaped tank (C1), 65% in ordinary storage tank (C2), while controlling the 35% are mixed at room temperature in the conduit.
The rectification section of the rectification tower (T1) is a two-step regular packing (12 theoretical plates), the stripping section is a one-stage random packing (three theoretical plates), and the residual oil supply position is , Between the 2nd and 3rd packings from the top, the vaporized vapor supply position is above the liquid level at the bottom of the column (the lower part of the 3rd packing), High-boiling heavy oil (that is, high-boiling hydrocarbons) flows out from the split oil (that is, low-boiling hydrocarbons) and steam, and from the bottom of the column. The reflux ratio at the top of the tower is 0.7, and the steam blown from the bottom of the tower is 5% (mass) of the heavy oil at the bottom of the tower, which lowers the partial pressure of the oil vapor and lowers the bottom temperature. .. The operating temperature at the bottom of the column is 225° C., the operating temperature at the top of the column is 113° C., and the operating pressure is 0.13 MPa. In the reflux tank (C3), the operating temperature is 40° C. and the operating pressure is 0.1 MPa.
The fractionated oil obtained by distillation is sent to the static mixer (M1). The mass ratio of oil entering the static mixer (M1) to fresh room temperature water is 4:1. In the static mixer (M1), the operating temperature is 37 to 38°C and the operating pressure is 0.6 MPa. Is.
In the gravity settling tank (C4), the operating temperature is 37° C. and the operating pressure is 0.25 MPa.
Both the hot material at the top of the tower and the hot material at the bottom of the tower are heat-exchanged with new raw material to perform heat integration, thereby recovering as much heat as possible and reducing the amount of cooling water used.
According to the above conditions, the yield of the distillate oil that can be recovered reaches 63.12%, which satisfies the raw material properties required by the downstream gasoline hydrogenation apparatus. When the bottom heavy oil and the sediment are blended, the property of the raw material required by the delayed coking device or the property of the fuel oil for marine residue is satisfied.
The residual filth oil required for Example 1 was relatively clean, the resulting water-washed distillate fraction was even cleaner, which is advantageous for reducing the amount of water used for rinsing. The phenomenon does not occur.
実施例２
化学工業における汚油残液の高効率浄化処理用の装置は、処理能力２ｔ／ｈであり、汚油残液には炭素粒子の固形分不純物が含まれ、且つアスファルテンが多い場合、まず蒸留すると、物質移動分離部材に垢が発生しやすく、長周期の運転に悪影響を及ぼす。蒸留を先に行う場合であっても、実施例２によれば、垢の発生を低減できるため、実施例２が好ましく、装置の安全性、運転の安定性が確保できる。
本例では、１５種類の廃油を供給混合原料とし、その中で、５種類の汚油残液は、低沸点軽質成分（標準密度８００ｋｇ／ｍ３未満）であり、５４質量％を占め、１０種類の汚油残液は、高沸点重質成分（標準密度８００ｋｇ／ｍ３超）であり、４６質量％を占めており、蒸留−水洗プロセスを用い、具体的な操作は、以下のとおりである。
球形タンク（Ｃ１）では、操作温度が２５℃、操作圧力が０．３５ＭＰａ、普通貯蔵タンク（Ｃ２）では、操作温度が２５℃、操作圧力が０ＭＰａである。流出流れの質量流量については、球形タンク（Ｃ１）では、５４％、普通貯蔵タンク（Ｃ２）では、４６％であるように制御しながら、管路において常温で混合する。
精留塔（Ｔ１）の精留部は、２段規則パッキング（理論段数１２段）であり、ストリッピング部は、１段ランダムパッキング（理論段数３段）であり、汚油残液供給位置は、上から第２段と第３段のパッキングの間にあり、放散蒸気供給位置は、塔底の液面の上方（第３段パッキングの下部）にあり、塔頂からは、低沸点留分油及び水蒸気、塔底からは、高沸点重質油が流出する。塔頂の還流比は、０．６７であり、塔底から吹き込まれる水蒸気は、塔底の重質油の５％（質量）であり、塔底の操作温度が２２７℃、塔頂の操作温度が１１５℃、操作圧力が０．１３ＭＰａである。還流タンク（Ｃ３）では、操作温度が４０℃、操作圧力が０．１ＭＰａである。
蒸留により得られた留分油は、静的混合器（Ｍ１）に送られる。静的混合器（Ｍ１）に入った油と新しい常温水との質量比は、４：１であり、静的混合器（Ｍ１）では、操作温度が３７〜３８℃、操作圧力が０．６ＭＰａである。
重力沈降タンク（Ｃ４）では、操作温度が３７℃、操作圧力が０．２５ＭＰａである。
上記条件によれば、回収可能な留分油の収率は、５２．１％に達し、下流のガソリン水素化装置により求められる原料の性質を満たすものの、指標の一部がぎりぎりで合格することとなる。塔底重質油及び沈降液をブレンドすると、遅延コーキング装置により求められる原料の性質を満たし、又は舶用残渣燃料油の性質を満たす。
Example 2
An apparatus for highly efficient purification treatment of waste oil residual liquid in the chemical industry has a processing capacity of 2 t/h, and when the waste oil residual liquid contains solid impurities of carbon particles and a large amount of asphaltene, first distill it. , Dust is easily generated on the mass transfer separation member, which adversely affects long-cycle operation. Even if the distillation is performed first, according to the second embodiment, since the generation of dust can be reduced, the second embodiment is preferable, and the safety of the device and the stability of the operation can be secured.
In this example, 15 kinds of waste oils were used as feed mixed raw materials, and among them, 5 kinds of waste oil residual liquids were low boiling point light components (standard density less than 800 kg/m 3 ) and occupied 54 mass%. The waste oil residual liquid of a kind is a high boiling point heavy component (standard density of more than 800 kg/m 3 ) and occupies 46% by mass. The distillation-water washing process is used, and the specific operation is as follows. is there.
In spherical-shaped tank (C1), operating temperature of 25 ° C., the operating pressure is 0.35 MPa, the ordinary storage tank (C2), operating temperature of 25 ° C., the operating pressure is 0 MPa. The mass flow rate of the effluent stream, the sphere-shaped tank (C1), 54% in ordinary storage tank (C2), while controlled to be 46%, are mixed at room temperature in the conduit.
The rectification section of the rectification tower (T1) is a two-step regular packing (12 theoretical plates), the stripping section is a one-stage random packing (three theoretical plates), and the residual oil supply position is , Between the 2nd and 3rd packings from the top, the vaporized vapor supply position is above the liquid level at the bottom of the column (the lower part of the 3rd packing), and the low boiling fraction High boiling heavy oil flows out from the oil and steam, and the bottom of the tower. The reflux ratio at the top of the column is 0.67, the water vapor blown from the bottom of the column is 5% (mass) of the heavy oil at the bottom of the column, the operating temperature of the column bottom is 227° C., the operating temperature of the column top. Is 115°C and the operating pressure is 0.13 MPa. In the reflux tank (C3), the operating temperature is 40° C. and the operating pressure is 0.1 MPa.
The fractionated oil obtained by distillation is sent to the static mixer (M1). The mass ratio of oil entering the static mixer (M1) to fresh room temperature water is 4:1. In the static mixer (M1), the operating temperature is 37 to 38°C and the operating pressure is 0.6 MPa. Is.
In the gravity settling tank (C4), the operating temperature is 37°C and the operating pressure is 0.25 MPa.
According to the above conditions, the yield of distillate oil that can be recovered reaches 52.1% and satisfies the raw material properties required by the downstream gasoline hydrogenation device, but some of the indicators pass at the last minute. Becomes When the bottom heavy oil and the sediment are blended, the properties of the raw material required by the delayed coking device or the properties of the residual fuel oil for ships are satisfied.
実施例３
化学工業における汚油残液の高効率浄化処理用の装置であって、本例では、１２種類の汚油残液を供給混合原料とし、その中で、３種類の汚油残液は、低沸点軽質成分（標準密度８００ｋｇ／ｍ３未満）であり、２１質量％であり、９種類の汚油残液は、高沸点重質成分（標準密度８００ｋｇ／ｍ３超）であり、そのうちの４種類の汚油残液は、超重質・超高粘度の多環芳香族炭化水素及びアスファルテン成分であり、７９質量％を占めており、混合後の原料は、標準密度１０６０ｋｇ／ｍ３、５０℃動粘度≦２０３ｍｍ２／ｓに達する。装置については、処理能力が１．６ｔ／ｈであり、蒸留−水洗プロセスを用い、具体的な操作は、以下のとおりである。
球形タンク（Ｃ１）では、操作温度が２５℃、操作圧力が０．３５ＭＰａ、普通貯蔵タンク（Ｃ２）では、操作温度が５７℃、操作圧力が０ＭＰａである。流出流れの質量流量については、球形タンク（Ｃ１）では、１６％、普通貯蔵タンク（Ｃ２）では、８４％であるように制御しながら、管路において常温で混合する。
精留塔（Ｔ１）の精留部は、２段規則パッキング（理論段数１２段）であり、ストリッピング部は、１段ランダムパッキング（理論段数３段）であり、汚油残液供給位置は、上から第２段と第３段のパッキングの間にあり、放散蒸気供給位置は、塔底の液面の上方（第３段のパッキングの下部）にあり、塔頂からは、低沸点の留分油及び水蒸気、塔底からは、高沸点の重質油が流出する。塔頂の還流比は、０．６８であり、塔底から吹き込まれる水蒸気は、塔底重質油の５％（質量）であり、油蒸気の分圧を低下させて塔底温度を低下させる。塔底の操作温度が２２５℃、塔頂の操作温度が１１４℃、操作圧力が０．１３ＭＰａである。還流タンク（Ｃ３）では、操作温度が４０℃、操作圧力が０．１ＭＰａである。
蒸留により得られた留分油は、一部が０．６７０２／ｈで循環分岐バルブを通過してり、重質原料と混合し、残りの一部が０．３６７ｔ／ｈで静的混合器（Ｍ１）に送られる。静的混合器（Ｍ１）に入った油と新しい常温水との質量比は、４：１であり、静的混合器（Ｍ１）では、操作温度が３７〜３８℃、操作圧力が０．６ＭＰａである。
重力沈降タンク（Ｃ４）では、操作温度が３７℃、操作圧力が０．２５ＭＰａである。
塔頂の熱い材料も塔底の熱い材料も新しい原料と熱交換し、熱統合を行い、それにより、できるだけ熱量を回収して、冷却水の使用量を低減させる。
上記条件によれば、超重質・超高粘度の汚油残液材料を処理して、回収可能な留分油収率は、２０．５８％に達し、下流のガソリン水素化装置により求められる原料の性質をたす。塔底重質油及び沈降液をブレンドすると、遅延コーキング装置により求められる原の性質を満たし、又は舶用残渣燃料油の性質を満たす。
Example 3
A device for highly efficient purification treatment of waste oil residual liquid in the chemical industry. In this example, 12 kinds of waste oil residual liquid are used as a feed mixed material, and among them, three kinds of waste oil residual liquid are low. It is a boiling point light component (standard density of less than 800 kg/m 3 ) and is 21% by mass, and 9 kinds of waste oil residual liquids are high boiling point heavy components (standard density of more than 800 kg/m 3 ), of which 4 The types of waste oil residual liquids are super-heavy and ultra-high-viscosity polycyclic aromatic hydrocarbons and asphaltene components, accounting for 79% by mass, and the raw materials after mixing have a standard density of 1060 kg/m 3 and 50°C A kinematic viscosity of ≦203 mm 2 /s is reached. Regarding the apparatus, the throughput is 1.6 t/h, the distillation-water washing process is used, and the specific operation is as follows.
In spherical-shaped tank (C1), operating temperature of 25 ° C., the operating pressure is 0.35 MPa, the ordinary storage tank (C2), operating temperature of 57 ° C., the operating pressure is 0 MPa. The mass flow rate of the effluent stream, the sphere-shaped tank (C1), 16% in ordinary storage tank (C2), while controlling the 84% are mixed at room temperature in the conduit.
The rectification section of the rectification tower (T1) is a two-step regular packing (12 theoretical plates), the stripping section is a one-stage random packing (three theoretical plates), and the residual oil supply position is , Between the second and third packings from the top, the vaporized vapor supply position is above the liquid level at the bottom of the column (lower part of the third packing), and from the top of the column, the low boiling point Heavy oil with a high boiling point flows out from the fractionated oil, steam, and the bottom of the column. The reflux ratio at the top of the column is 0.68, and the steam blown from the bottom of the column is 5% (mass) of the heavy oil at the bottom of the column, which lowers the partial pressure of the oil vapor and lowers the bottom temperature. .. The operating temperature at the bottom of the column is 225°C, the operating temperature at the top of the column is 114°C, and the operating pressure is 0.13 MPa. In the reflux tank (C3), the operating temperature is 40° C. and the operating pressure is 0.1 MPa.
A part of the distillate oil obtained by distillation passed through the circulation branch valve at 0.6702/h and was mixed with the heavy raw material, and the remaining part was at 0.367 t/h in the static mixer. (M1). The mass ratio of oil entering the static mixer (M1) to fresh room temperature water is 4:1. In the static mixer (M1), the operating temperature is 37 to 38°C and the operating pressure is 0.6 MPa. Is.
In the gravity settling tank (C4), the operating temperature is 37° C. and the operating pressure is 0.25 MPa.
Both the hot material at the top of the tower and the hot material at the bottom of the tower are heat-exchanged with new raw material to perform heat integration, thereby recovering as much heat as possible and reducing the amount of cooling water used.
According to the above conditions, a distillate oil yield that can be collected by treating an ultra-heavy/ultra-high-viscosity waste oil residual material reaches 20.58%, and is a raw material required by a downstream gasoline hydrogenator. The nature of. Blending the bottoms heavy oil and the sediment will meet the original properties required by the delayed coking unit or the properties of the residual fuel oil for ships.
本発明の上記実施例は、汚油残液の性質に応じて異なる操作プロセスを切り替えることによって、汚油残液の利用率を向上させ、汚油残液における高品質成分を十分に利用して、環境汚染を低減させることができる。また、全精留塔を分離装置とするため、占有する面積を低減させて、設備投資を低下させ、さらに塔底の熱量に対して熱統合を行うことでエネルギーの利用を最大化させる。また、汚油残液の供給源の量にはバランスがよくなくて非連続性もあるため、性質の差異が大きいという特徴があることを考慮して、塔頂留分油が戻るための原料パイプライン、即ち分岐バルブ（Ｖ７）を増設し、それによって、正常に分離処理できるように汚油残液組成の性質を調整できる。 The above-described embodiment of the present invention improves the utilization rate of the waste oil residual liquid by switching between different operation processes depending on the properties of the waste oil residual liquid, and makes full use of the high-quality components in the waste oil residual liquid. The environmental pollution can be reduced. Moreover, since all the rectification columns are used as a separation device, the area occupied is reduced, the capital investment is reduced, and the energy utilization is maximized by performing heat integration with the heat quantity at the bottom of the column. In addition, since the balance of the amount of residual oil residual liquid is not well-balanced and there is discontinuity, the fact that there is a large difference in properties is considered as a raw material for returning the overhead fraction oil. By adding a pipeline, that is, a branch valve (V7), it is possible to adjust the properties of the residual oil residual liquid composition so that the separation process can be performed normally.
本明細書における各実施例は、漸進的な形で説明されており、各実施例については、ほかの実施例との相違点が重点として説明され、各実施例の間の同じ又は類似した部分は、互いに参照すればよい。実施例で開示された装置に関しては、実施例で開示された方法に対応するため、簡単に説明し、関連する内容については、方法の部分についての説明を参照すればよい。 Each example in this specification is described in a progressive manner, and each example is described by focusing on differences from other examples, and the same or similar parts between each example Can refer to each other. Since the apparatus disclosed in the embodiments corresponds to the method disclosed in the embodiments, a brief description will be given, and for related contents, the description of the method portion may be referred to.
開示された実施例の上記説明により、当業者が本発明を実現又は利用することができる。これら実施例に対するさまざまな修正は、当業者にとって明らかなことであり、本明細書に定義された一般的な原理は、本発明の趣旨又は範囲から逸脱せずにほかの実施例においても実現できる。したがって、本発明は、本明細書に示されるこれら実施例に制限されず、本明細書に開示された原理及び新規性と一致する最も広範な範囲と合致する。 Given the above description of the disclosed embodiments, those skilled in the art can implement or use the present invention. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the invention. .. Therefore, the present invention is not limited to these examples provided herein, but is consistent with the broadest scope consistent with the principles and novelty disclosed herein.
Claims (7)
貯蔵設備、蒸留分離設備、静的混合設備、重力沈降設備を備え、
前記貯蔵設備は、軽質易揮発性汚油残液を貯蔵するための球形タンク（Ｃ１）と、重質難揮発性汚油残液を貯蔵するための普通貯蔵タンク（Ｃ２）とを備え、前記球形タンク（Ｃ１）には、清澄液を排出するための第１排出口が設けられ、前記普通貯蔵タンク（Ｃ２）には、清澄液を排出するための第２排出口が設けられ、前記第１排出口は、第１ポンプ（Ｐ１）を介して第１熱交換器（Ｅ１）の入り口側に接続され、前記第２排出口は、第２ポンプ（Ｐ２）を介して前記第１熱交換器（Ｅ１）の入り口側に接続され、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）が前記第１熱交換器（Ｅ１）に接続される共通管路には、第１バルブ（Ｖ１）が設けられ、
前記蒸留分離設備は、精留塔（Ｔ１）を備え、前記精留塔（Ｔ１）の内部には、塔頂に位置する塔頂気相排出口、塔外周面に位置する清澄液供給口及び塔底に位置する塔底液相排出口が設けられ、前記第１熱交換器（Ｅ１）の出口側が第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して前記清澄液供給口に接続され、前記塔頂気相排出口は、前記第１熱交換器（Ｅ１）を介して還流タンク（Ｃ３）の入り口に接続され、前記精留塔（Ｔ１）には、塔頂還流口がさらに設けられ、前記還流タンク（Ｃ３）は、還流ポンプ（Ｐ３）を介して前記塔頂還流口に接続されて、塔頂の温度を調整して塔頂留出油に要求される品質を制御する液相還流を形成させ、
前記静的混合設備は、静的混合器（Ｍ１）を備え、前記静的混合器（Ｍ１）には、油類入り口、洗浄水入り口及び油水混合物出口が設けられ、前記第１ポンプ（Ｐ１）、第２ポンプ（Ｐ２）は、また同一管路を介して該油類入り口に接続され、該同一管路には、第２バルブ（Ｖ２）が設けられ、前記還流タンク（Ｃ３）は、管路を介して該油類入り口に接続され、還流タンク（Ｃ３）と該油類入り口との間には、第３バルブ（Ｖ３）が設けられ、
前記重力沈降設備は、重力沈降タンク（Ｃ４）を備え、前記重力沈降タンク（Ｃ４）には、タンク上面に位置する気相排出口及び油水混合物入り口、タンク下面に位置する清澄液を排出するための第３排出口及び油含有汚水排出口が設けられ、前記油水混合物入り口は、管路を介して前記油水混合物出口に接続され、前記第３排出口は、順次第５ポンプ（Ｐ５）、第４バルブ（Ｖ４）を介して前記第１熱交換器（Ｅ１）に接続され、前記第４バルブ（Ｖ４）に接続されていない前記第５ポンプ（Ｐ５）の管路には、第５バルブ（Ｖ５）が設けられ、前記塔頂気相排出口は、管路を介して前記第５バルブ（Ｖ５）の出口に接続され、前記塔頂気相排出口と前記第５バルブ（Ｖ５）の出口との間の管路には、第６バルブ（Ｖ６）が設けられる、
ことを特徴とする化学工業における汚油残液の高効率浄化処理用の分離装置。 A separation device for high-efficiency purification treatment of waste oil residual liquid in the chemical industry,
Equipped with storage equipment, distillation separation equipment, static mixing equipment, gravity settling equipment,
The storage facility is provided with a spherical-shaped tank for storing a light volatile dirty oil residual liquid (C1), and a common storage tank for storing the heavy flame volatile dirty oil residual liquid (C2), the front Symbol sphere shape tank (C1), a first outlet for discharging the clarified liquid is provided, wherein the common storage tank (C2), a second outlet for discharging the clarified liquid is provided , The first outlet is connected to the inlet side of the first heat exchanger (E1) via a first pump (P1), and the second outlet is connected to the first side via a second pump (P2). The first pipe is connected to the inlet side of the first heat exchanger (E1), and the first pump (P1) and the second pump (P2) are connected to the first heat exchanger (E1). A valve (V1) is provided,
The distillation separation equipment includes a rectification column (T1), and inside the rectification column (T1), a top gas phase outlet located at the top of the column, a clear liquid supply port located on the outer peripheral surface of the column, and A bottom liquid phase outlet located at the bottom of the tower is provided, and the outlet side of the first heat exchanger (E1) passes through the second heat exchanger (E2) and the third heat exchanger (E3) to obtain the clarified liquid. The top gas phase outlet is connected to the inlet, and is connected to the inlet of the reflux tank (C3) through the first heat exchanger (E1). A reflux port is further provided, and the reflux tank (C3) is connected to the overhead reflux port via a reflux pump (P3) to adjust the temperature at the top of the column and is required for overhead distillate oil. Form a liquid phase reflux that controls the quality,
The static mixing equipment comprises a static mixer (M1), the static mixer (M1) is provided with an oil inlet, a wash water inlet and an oil/water mixture outlet, and the first pump (P1). , The second pump (P2) is also connected to the oil inlet through the same pipeline, a second valve (V2) is provided in the same pipeline, and the reflux tank (C3) is a pipe. A third valve (V3) is provided between the reflux tank (C3) and the oil inlet, which is connected to the oil inlet through a passage.
The gravity settling equipment includes a gravity settling tank (C4), and the gravity settling tank (C4) discharges a gas phase discharge port and an oil/water mixture inlet located on the upper surface of the tank, and a clearing liquid located on the lower surface of the tank. A third outlet and an oil-containing wastewater outlet are provided, the oil-water mixture inlet is connected to the oil-water mixture outlet through a pipe, and the third outlet is sequentially connected to a fifth pump (P5), A fifth valve (P5) is connected to the first heat exchanger (E1) through a four valve (V4) and is not connected to the fourth valve (V4). V5) is provided, and the top gas phase discharge port is connected to the outlet of the fifth valve (V5) via a pipeline, and the top gas phase discharge port and the outlet of the fifth valve (V5) are provided. A sixth valve (V6) is provided in the pipeline between
A separation device for highly efficient purification treatment of waste oil residual liquid in the chemical industry.
ことを特徴とする請求項１に記載の化学工業における汚油残液の高効率浄化処理用の装置。 The rectification tower (T1) comprises a rectification section and a stripping section, a high-performance packing separation member is used in the rectification section, and a large-capacity random packing capable of preventing coking is provided in the stripping section. used,
The apparatus for highly efficient purification treatment of waste oil residual liquid in the chemical industry according to claim 1.
ことを特徴とする請求項２に記載の化学工業における汚油残液の高効率浄化処理用の装置。 The bottom of the rectification column (T1 ) is further provided with a desorption steam inlet (S1) ,
The apparatus for highly efficient purification treatment of a waste oil residual liquid in the chemical industry according to claim 2, wherein.
ことを特徴とする請求項１に記載の化学工業における汚油残液の高効率浄化処理用の装置。 A branch valve (V7) is provided between the first valve (V1) and the third valve (V3), and when the branch valve (V7) is opened, it is distilled from the rectification column (T1). A portion of the low boiling hydrocarbons material mixes with the clarified liquid from the first valve (V1) via the branch valve (V7),
The apparatus for highly efficient purification treatment of waste oil residual liquid in the chemical industry according to claim 1.
請求項１〜４のいずれか１項に記載の装置を用いて、処理対象となる化学工業における汚油残液の性質に応じて、蒸留−水洗及び／又は水洗−蒸留処理方法を実施する、
ことを特徴とする化学工業における汚油残液の高効率浄化処理用の方法。 A method for highly efficient purification treatment of residual oil from a chemical industry,
Using the apparatus according to any one of claims 1 to 4, a distillation-water washing and/or a water washing-distillation treatment method is carried out according to the property of the residual oil residue in the chemical industry to be treated.
The method for efficient purification treatment of dirty oil residual liquid in the chemical industry characterized the this.
第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を開け、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を閉め、第１ポンプ（Ｐ１）を起動させて球形タンク（Ｃ１）における清澄液を吸い出すとともに、第２ポンプ（Ｐ２）を起動させて普通貯蔵タンク（Ｃ２）における清澄液を吸い出すステップと、
生産の要求に対応する割合で球形タンク（Ｃ１）及び普通貯蔵タンク（Ｃ２）から吸い出された清澄液を混合し、順次第１熱交換器（Ｅ１）、第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して混合後の清澄液を精留塔（Ｔ１）に送り、前記精留塔（Ｔ１）で前記清澄液を蒸留処理し、発生させた低沸点炭化水素類物質及び水蒸気を凝縮させて冷却させた後、還流タンク（Ｃ３）に送り、一部の低沸点炭化水素類物質を還流ポンプ（Ｐ３）で精留塔（Ｔ１）のトップに戻し、還流タンク（Ｃ３）からの低沸点炭化水素類物質をさらに静的混合器（Ｍ１）に送るステップと、
前記静的混合器（Ｍ１）に水を加えて、低沸点炭化水素類物質と水を所定の割合で静的混合器（Ｍ１）において混合して洗浄を行い、洗浄して得られた油水混合物を重力沈降タンク（Ｃ４）に送り、さらに重力沈降タンク（Ｃ４）による不均一相分離により水洗のステップを完了するステップと、を含み、
前記水洗−蒸留処理方法は、
第１バルブ（Ｖ１）、第３バルブ（Ｖ３）、第５バルブ（Ｖ５）を閉め、第２バルブ（Ｖ２）、第４バルブ（Ｖ４）、第６バルブ（Ｖ６）を開け、第１ポンプ（Ｐ１）を起動させて球形タンク（Ｃ１）における清澄液を吸い出すとともに、第２ポンプ（Ｐ２）を起動させて普通貯蔵タンク（Ｃ２）における清澄液を吸い出すステップと、
生産の要求に対応する割合で球形タンク（Ｃ１）及び普通貯蔵タンク（Ｃ２）から吸い出された清澄液を混合し、混合後の清澄液を静的混合器（Ｍ１）に入れるステップと、
前記静的混合器（Ｍ１）に水を加えて、前記混合後の清澄液と水を所定の割合で静的混合器（Ｍ１）において混合して洗浄を行い、洗浄して得られた油水混合物を重力沈降タンク（Ｃ４）に送り、さらに重力沈降タンク（Ｃ４）による不均一分離により水洗のステップを完了し、順次第１熱交換器（Ｅ１）、第２熱交換器（Ｅ２）、第３熱交換器（Ｅ３）を介して水洗後の清澄液を精留塔（Ｔ１）に送り、精留塔（Ｔ１）で蒸留処理し、低沸点炭化水素類物質と高沸点炭化水素類物質に分離させ、蒸留分離ステップを完了するステップと、を含む、
ことを特徴とする請求項５に記載の化学工業における汚油残液の高効率浄化処理用の方法。 The distillation-water washing treatment method,
The first valve (V1), the third valve (V3) and the fifth valve (V5) are opened, the second valve (V2), the fourth valve (V4) and the sixth valve (V6) are closed, and the first pump ( P1) was allowed to start with sucking the clarified liquid in the sphere-shaped tank (C1), a step of sucking out the clarified liquid in the common storage tank (C2) activates the second pump (P2),
Clarified liquid that has been sucked out of the sphere-shaped tank (C1) and common storage tank (C2) at a rate corresponding to the request of producing mixed, order soon first heat exchanger (E1), a second heat exchanger (E2) , The low-boiling hydrocarbons generated by sending the mixed clarified liquid to the rectification column (T1) through the third heat exchanger (E3) and subjecting the clarified liquid to distillation treatment in the rectification column (T1). After the similar substances and water vapor are condensed and cooled, they are sent to a reflux tank (C3), and some low-boiling point hydrocarbon substances are returned to the top of the rectification column (T1) by a reflux pump (P3), and then the reflux tank. Sending the low boiling hydrocarbons material from (C3) to a static mixer (M1);
Water is added to the static mixer (M1), low-boiling hydrocarbon substances and water are mixed in a predetermined ratio in the static mixer (M1) for washing, and an oil-water mixture obtained by washing To the gravity settling tank (C4) and further completing the washing step by heterogeneous phase separation by the gravity settling tank (C4).
The water washing-distillation treatment method,
The first valve (V1), the third valve (V3) and the fifth valve (V5) are closed, the second valve (V2), the fourth valve (V4) and the sixth valve (V6) are opened, and the first pump ( P1) was allowed to start with sucking the clarified liquid in the sphere-shaped tank (C1), a step of sucking out the clarified liquid in the common storage tank (C2) activates the second pump (P2),
Clarified liquid that has been sucked out of the sphere-shaped tank (C1) and common storage tank (C2) at a rate corresponding to the request of producing mixed, a step of placing a clear solution after mixing in a static mixer (M1),
Water is added to the static mixer (M1), and the clarified liquid after mixing and water are mixed in a predetermined ratio in the static mixer (M1) for washing, and an oil-water mixture obtained by washing To the gravity settling tank (C4), and the step of washing with water is completed by non-uniform separation by the gravity settling tank (C4). The first heat exchanger (E1), the second heat exchanger (E2) and the third The clarified liquid after washing with water is sent to the rectification column (T1) through the heat exchanger (E3) and subjected to distillation treatment in the rectification column (T1) to separate into low boiling point hydrocarbons substances and high boiling point hydrocarbons substances. And completing the distillation separation step,
The method for highly efficient purification treatment of waste oil residual liquid in the chemical industry according to claim 5, characterized in that.
前記精留塔（Ｔ１）では、操作温度が常温４０〜３００℃、操作圧力が０〜０．５ＭＰａであり、
前記静的混合器（Ｍ１）では、操作温度が２〜８０℃、操作圧力が０〜０．８ＭＰａであり、
前記重力沈降タンク（Ｃ４）では、操作温度が２〜８０℃、操作圧力が０〜０．５ＭＰａであり、
前記還流タンク（Ｃ３）では、操作温度が２〜６０℃、操作圧力が０〜０．５ＭＰａである、
ことを特徴とする請求項５に記載の化学工業における汚油残液の高効率浄化処理用の方法。 Operation temperature before Symbol sphere shape tank (C1) is, 1 to 70 ° C., ordinary operating temperature of the storage tank (C2) is, 1 to 100 ° C., the ball shape tank (C1), the ordinary storage tank (C2) The operating pressure is 0 to 0.8 MPa,
In the rectification column (T1), the operating temperature is room temperature 40 to 300° C., the operating pressure is 0 to 0.5 MPa,
In the static mixer (M1), the operating temperature is 2 to 80° C., the operating pressure is 0 to 0.8 MPa,
In the gravity settling tank (C4), the operating temperature is 2 to 80° C., the operating pressure is 0 to 0.5 MPa,
In the reflux tank (C3), the operating temperature is 2 to 60° C., and the operating pressure is 0 to 0.5 MPa.
The method for highly efficient purification treatment of waste oil residual liquid in the chemical industry according to claim 5, characterized in that.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911331140.6 | 2019-12-20 | ||
| CN201911331140.6A CN111135597B (en) | 2019-12-20 | 2019-12-20 | Separation device and method for efficiently and cleanly treating chemical waste oil residual liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP6739829B1 true JP6739829B1 (en) | 2020-08-12 |
| JP2021098184A JP2021098184A (en) | 2021-07-01 |
Family
ID=70519255
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2020011632A Active JP6739829B1 (en) | 2019-12-20 | 2020-01-28 | Separation apparatus and method for highly efficient purification treatment of waste oil residual liquid in chemical industry |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JP6739829B1 (en) |
| CN (1) | CN111135597B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114225476A (en) * | 2022-01-19 | 2022-03-25 | 智火柴科技(深圳)有限公司 | Bubble eliminating device for oil liquid oil path |
| CN114534278A (en) * | 2020-11-10 | 2022-05-27 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
| CN116212430A (en) * | 2023-03-20 | 2023-06-06 | 重庆中润新材料股份有限公司 | Ammonia water recovery system |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114100172B (en) * | 2021-10-27 | 2022-12-27 | 中国石油化工股份有限公司 | Treatment method of chemical residual liquid |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3769043B2 (en) * | 1994-12-19 | 2006-04-19 | 日揮株式会社 | Treatment method of hydrocarbon-containing gas |
| US5738762A (en) * | 1995-03-08 | 1998-04-14 | Ohsol; Ernest O. | Separating oil and water from emulsions containing toxic light ends |
| CN200955422Y (en) * | 2006-09-06 | 2007-10-03 | 王庆生 | Oil-purifying apparatus |
| CN101812320B (en) * | 2009-08-14 | 2013-02-06 | 李宝东 | Waste oil regenerated energy device and processing method |
| CN104556513B (en) * | 2013-10-15 | 2016-08-17 | 中国石油化工股份有限公司 | Dirty oil dewatering process and device |
| CN104711008B (en) * | 2015-03-12 | 2017-12-22 | 中国石油化工股份有限公司 | A kind of device for preventing oil distillation column salt crust |
| CN106336886B (en) * | 2016-11-04 | 2017-11-17 | 成都西南石大石油工程技术有限公司 | A kind of industrial waste oil extraction equipment and its application method containing solid particle |
| CN206355622U (en) * | 2016-12-20 | 2017-07-28 | 杜彪 | A kind of PETROLEUM PROCESSING rectifying column |
| CN106929095A (en) * | 2017-01-24 | 2017-07-07 | 玉门市润泽环保再生能源新技术有限公司 | A kind of waste mineral oil processing method |
| CN108929718B (en) * | 2017-05-26 | 2020-12-01 | 中国石油天然气股份有限公司 | Desalting system and crude oil desalting method |
| CN109355087B (en) * | 2018-11-21 | 2021-01-15 | 陕西延长石油（集团）有限责任公司 | Step recovery device and method for oil product in gas containing oil dust |
| CN109880648B (en) * | 2019-04-10 | 2021-04-02 | 上海思九科技发展有限公司 | Fractionating tower circulating device and water washing method |
-
2019
- 2019-12-20 CN CN201911331140.6A patent/CN111135597B/en active Active
-
2020
- 2020-01-28 JP JP2020011632A patent/JP6739829B1/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114534278A (en) * | 2020-11-10 | 2022-05-27 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
| CN114534278B (en) * | 2020-11-10 | 2024-03-15 | 宝武碳业科技股份有限公司 | Benzene hydrogenation pre-evaporation system with online cleaning function, process and application |
| CN114225476A (en) * | 2022-01-19 | 2022-03-25 | 智火柴科技(深圳)有限公司 | Bubble eliminating device for oil liquid oil path |
| CN116212430A (en) * | 2023-03-20 | 2023-06-06 | 重庆中润新材料股份有限公司 | Ammonia water recovery system |
| CN116212430B (en) * | 2023-03-20 | 2023-09-26 | 重庆中润新材料股份有限公司 | Ammonia water recovery system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111135597B (en) | 2021-02-05 |
| CN111135597A (en) | 2020-05-12 |
| JP2021098184A (en) | 2021-07-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6739829B1 (en) | Separation apparatus and method for highly efficient purification treatment of waste oil residual liquid in chemical industry | |
| CN104151119B (en) | The method of octane-iso is prepared in the deep processing of a kind of carbon four | |
| KR101475068B1 (en) | A process and an appratus for water quenching a pyrolysis furnace effluent | |
| CN112048330B (en) | Process and device for reducing coke powder of delayed coking fractionating tower | |
| CN109384341A (en) | Semi-coke high concentrated organic wastewater recycling treatment system and method | |
| CN107177372B (en) | The suspended bed hydrogenation method and hydrogenation system of heavy oil feedstock | |
| JP2014527572A (en) | Delayed coking of oil residues | |
| CN113773874B (en) | High aromatic hydrocarbon oil material and preparation method and application thereof | |
| CN113755208B (en) | High aromatic hydrocarbon oil material and preparation method and application thereof | |
| CN107400536A (en) | Coking, absorbing and stabilizing technique and system | |
| CN113897220B (en) | High aromatic hydrocarbon oil material and preparation method and application thereof | |
| CN113717754B (en) | Catalytic cracking process for producing high aromatic hydrocarbon oil and high yield liquefied gas | |
| CN113717753B (en) | High aromatic hydrocarbon oil material and preparation method and application thereof | |
| CN112999815B (en) | Device and method for heat exchange washing of oil gas | |
| CN108384577A (en) | A kind of pre- hydrogenation unit of joint aromatics production line | |
| CN210462963U (en) | Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking | |
| CN114426860A (en) | Heavy oil supercritical extraction separation method and device | |
| CN107400537B (en) | A kind of coking, absorbing and stabilizing technique and device | |
| CN1141361C (en) | Catalytic cracking process for reducing content of olefin in gasoline | |
| CN114100172B (en) | Treatment method of chemical residual liquid | |
| CN113999690B (en) | Device and method for pyrolysis treatment of coal tar fluidized bed | |
| KR102552143B1 (en) | METHOD AND APPARATUS FOR PREPARING n-HEXANE | |
| CN116286084B (en) | Method for dearomatizing straight-run diesel oil fraction | |
| KR102629124B1 (en) | METHOD AND APPARATUS FOR PREPARING n-HEXANE | |
| US1917895A (en) | Method and apparatus for condensing and purifying vapors and gases |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20200128 |
|
| A871 | Explanation of circumstances concerning accelerated examination |
Free format text: JAPANESE INTERMEDIATE CODE: A871 Effective date: 20200128 |
|
| A975 | Report on accelerated examination |
Free format text: JAPANESE INTERMEDIATE CODE: A971005 Effective date: 20200310 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20200324 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20200525 |
|
| 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: 20200714 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20200716 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 6739829 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |
|
| R250 | Receipt of annual fees |
Free format text: JAPANESE INTERMEDIATE CODE: R250 |