WO2018084460A1 - 불포화 알데하이드 및 불포화 카르복실산의 제조 방법 - Google Patents
불포화 알데하이드 및 불포화 카르복실산의 제조 방법 Download PDFInfo
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- WO2018084460A1 WO2018084460A1 PCT/KR2017/011476 KR2017011476W WO2018084460A1 WO 2018084460 A1 WO2018084460 A1 WO 2018084460A1 KR 2017011476 W KR2017011476 W KR 2017011476W WO 2018084460 A1 WO2018084460 A1 WO 2018084460A1
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- catalyst bed
- unsaturated carboxylic
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- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
- C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
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- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
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- B01J19/0053—Details of the reactor
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- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
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- B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
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- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
- C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
- C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
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- C07C47/20—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms
- C07C47/21—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
- C07C47/22—Acryaldehyde; Methacryaldehyde
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- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
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- B01J2208/00017—Controlling the temperature
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- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00238—Adjusting the heat-exchange profile by adapting catalyst tubes or the distribution thereof, e.g. by using inserts in some of the tubes or adding external fins
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Definitions
- the present invention relates to a process for producing unsaturated aldehydes and unsaturated carboxylic acids.
- a multi-tubular L-and-tube reactor in the form of a heat exchanger is a type of reactor used for the purpose of efficiently removing the heat generated by the reaction.
- a solid catalyst is layered on a plurality of reaction streams, the raw material gas is supplied to the reaction tube to generate a chemical reaction to obtain a desired component, and the heat medium is transferred to the reaction reactor shell so that the chemical reaction can be optimally performed.
- Patent Document 1 Republic of Korea Patent Publication No. 2006-009 4 87 4 (2006.08.30)
- Patent Document 2 Republic of Korea Patent Publication No. 2012-0079617 (2012.07.13)
- the present invention is to provide a process for preparing unsaturated aldehydes and unsaturated carboxylic acids, which exhibits improved yield and operational stability by effectively controlling the reaction heat.
- At least one compound selected from propylene, isobutylene, t-butyl alcohol, and methyl-t-butyl ether is used as a raw material, using a multi-shell shell-and-leuve reaction device in a fixed bed multistage heat medium circulation type in which a catalyst is layered. And a method for producing unsaturated aldehydes and unsaturated carboxylic acids for the above raw materials by vapor phase contact oxidation with molecular oxygen or molecular oxygen-containing gas;
- the shell-and-tube reactor of the multi-stage heating medium circulation system includes a cylindrical shell, a plurality of tube sheets separating the inside of the shell into a plurality of independent spaces, and two spaces each having a plurality of independent spaces inside the shell.
- the heat transfer to the reaction tube is made at a temperature of 280 to 400 ° C each independently by the flow of independent heat medium;
- the reaction chamber has at least four fixed catalyst bed zones that are spatially continuous, and the fixed catalyst bed zone has high activity from the inlet to the outlet of the reaction tube.
- the term "comprising 11" embodies a particular characteristic, region, integer, step, operation, element, and / or component, and other specific characteristics, region, integer, step, operation, element, component, and / or group.
- At least one compound selected from propylene, isobutylene, t-butyl alcohol, and methyl-t-butyl ether is used as a raw material, using a multi-shell shell-and-tube reactor in which a catalyst is layered in a fixed bed multistage heat medium circulation method. And a method for producing unsaturated aldehydes and unsaturated carboxylic acids for the above raw materials by vapor phase contact oxidation with molecular oxygen or molecular oxygen-containing gas;
- the shell-and-tube reactor of the multi-stage heating medium circulation method includes a cylindrical shell, a plurality of rib sheets for separating the inside of the shell into a plurality of independent spaces, and two spaces each having a plurality of independent spaces inside the shell.
- the reaction chamber has at least four fixed catalyst bed zones that are spatially continuous, and the fixed catalyst bed zone has a high activity from the inlet to the outlet of the reaction tube.
- a plurality of rib sheets for separating the inside of the shell into a plurality of independent spaces, a baffle for dividing the plurality of independent spaces inside the shell into two spatially continuous regions, and
- a plurality of reaction tubes fixed to the inside of the shell through the plurality of rib sheets and baffles
- the inside of the shell is separated into a plurality of spaces independent by the plurality of the rib sheets, and the plurality of spaces are each independently heat-transferd to the semi-ungle ribs at a temperature of 280 to 400 ° C by an independent heating medium flow. .
- heat transfer to the reaction chamber is performed by a flow of independent multi-stage heating medium having high silver from the inlet to the outlet of the reaction tube.
- the tube sheet separates the inner space of the shell to allow control of the reaction temperature by an independent heating medium.
- a plurality of independent spaces inside the shell are provided with annular conduits connected to the heat medium supply ducts and annular conduits connected to the discharge ducts, thereby enabling the flow of each independent heat medium.
- the raw material gas is supplied through a supply duct connected to the plurality of reaction tubes, and is collected again after passing through the plurality of reaction tubes and discharged through the outlet duct.
- a molten salt containing nitrate and / or nitrite may be used as the heat medium.
- a case where the inside of the shell is divided into two independent spaces will be described as a representative example.
- this is presented as one embodiment according to the present invention, and various modifications are possible within the scope of the invention without intending to limit the scope of the rights thereby representative examples of the unsaturated aldehyde and unsaturated carboxylic acid In the shell-and-ryub Banunggi, where the manufacturing method is carried out,
- the plurality of rib sheets separate the interior of the shell into two independent spaces
- Two spaces separated by the plurality of rib sheets are divided into two zones each spatially continuous by the baffle;
- the fixed catalyst bed zone includes first to fourth fixed catalyst bed zones having high activity in the inlet to outlet direction of the reaction chamber, and the first fixed catalyst bed zone has the catalytic activity of the fourth failure catalyst bed zone. It can have an activity of 75 to 85% of.
- the first fixed catalyst bed zone exhibits an activity that is 75 to 85% of the catalytic activity of the fourth fixed catalyst bed zone;
- the second fixed catalyst bed zone represents an activity that is 85 to 95% of the catalytic activity of the fourth fixed catalyst bed zone;
- the third fixed catalyst layer zone may exhibit an activity that is 95 to 98% of the catalytic activity of the fourth fixed catalyst layer zone, and may be advantageous for securing improved yield and operational stability.
- heat is transferred to the reaction chamber at a temperature of 295 to 350 ° C. by the flow of the first heating medium;
- heat transfer to the rounding tube may be performed with a silver of 300 to 400 ° C. by the flow of the second heat medium.
- the temperature of the hot spot is performed by conducting heat transfer to the reaction chamber through independent multistage heat medium circulation to the reaction chamber and introducing a fixed catalyst bed zone having high activity from the inlet to the outlet of the reaction tube. It can control high efficiency and ensure high number and driving stability.
- the catalytic activity of the fixed catalyst bed zone can be controlled by adjusting the size of the catalyst to be layered, the occupying volume of the catalyst, the type of alkali metal, the content ratio of the alkali metal, the firing temperature and the like.
- the catalyst may be a composite metal oxide represented by Formula 1 below:
- Mo is molybdenum
- Bi bismuth
- M 1 is at least one element selected from the group consisting of W, Sb, As, P, Sn, and Pb,
- M 2 is at least one element selected from the group consisting of Fe, Zn, Cr, Mn, Cu, Pd, Ag, and Ru,
- M 3 is at least one element selected from the group consisting of Co, Cd, Ta, Pt, and Ni,
- ISA / KR M 4 is at least one element selected from the group consisting of Al, Zr, V, and Ce
- M 5 is at least one element selected from the group consisting of Se, Ga, Ti, Ge, Rh, and Au,
- M 6 is at least one element selected from the group consisting of Na, K, Li, Rb, Cs, Ca, Mg, Sr, and Ba,
- a, b, c, ⁇ , e, i, g, h, and i are the atomic ratios of each element
- the raw material compound used in the formation of the catalyst there is no particular limitation on the raw material compound used in the formation of the catalyst, and it can be applied in combination of ammonium salts, nitrates, carbonates, chlorides, lactates, hydroxides, organic acid salts, oxides, or combinations thereof.
- the preparation of the catalyst may include preparing a suspension in which the raw material compound is dissolved or dispersed in water; Drying the suspension to obtain a solid; Shaping the solid into a suitable shape; And it may be carried out by a method comprising the step of firing the molded solid.
- the catalyst may be used by being supported on an inert carrier.
- the step of supporting the suspension in contact with the inert carrier before carrying out the drying step may be further performed.
- the shape of the catalyst there is no particular limitation on the shape of the catalyst, and spherical, cylindrical (cylindrical), hollow cylindrical, ring-shaped, and irregular rounds may be applied.
- the shape of the catalyst layered in the fixed catalyst bed zone may be the same or different in black color (e.g., spherical catalyst at the inlet of the reaction stream, pellet catalyst at the outlet of the reaction tube). In general, however, it is preferable to layer the catalyst having the same shape.
- the catalyst preferably has a ratio (L / D) of the length (L) and the outer diameter (D) of the catalyst in the range of 0.5 to 1.3; In the case of columnar and spherical the outer diameter (D) of the catalyst is preferably 3 to 10 mm.
- the firing may be performed for 1 to 10 hours at a temperature of 300 to 600 ° C. under a stream of 0.2 to 2 m / s.
- the firing may be performed under a noble gas, an oxidizing atmosphere, or a reducing atmosphere.
- the reaction conditions of the gas phase catalytic oxidation are based on at least one compound selected from propylene, isobutylene, t-butyl alcohol, and methyl-t-butyl ether, and molecular oxygen Or by gas phase catalytic oxidation with a molecular oxygen-containing gas, which may be applied under conventional conditions in the process for producing unsaturated aldehydes and unsaturated carboxylic acids.
- gaseous traces containing propylene having a space velocity of 90 hr-i or more, 10-20% by volume of molecular oxygen, and inert gases (eg, nitrogen, carbon dioxide, water vapor, etc.) serving as 60-80% by volume of diluent
- inert gases eg, nitrogen, carbon dioxide, water vapor, etc.
- the intended reaction can be carried out by bringing the mixture into contact with the catalyst at a temperature of 250 to 500 ° C. and a pressure of 0.1 to 3 kg / cm 'G, a space velocity of 300 to 5000 hr STP for the total flow rate).
- Solution (1) was prepared by dissolving 1,000 g of ammonium molybdate while heating and stirring 2,500 ml of distilled water at 70 to 85 ° C.
- Solution (3) was prepared by dissolving 1097 g of cobalt nitrate in 200 ml of distilled water.
- the catalyst suspension was dried to obtain a catalyst solid, which was ground to a particle size of 150 or less.
- the ground catalyst powder was mixed for 2 hours and then molded into a cylinder having an outer diameter (D) of 7.0 mm and a length (L) of 7.7 mm.
- the content of potassium nitrate is adjusted to 3.76 g;
- the catalyst powder is shaped into a cylinder having an outer diameter (D) of 6.0 mm and a length (L) of 6.5 mm; Except that this was calcined for 5 hours under 470 ° C in an air atmosphere,
- the content of the color nitrate is adjusted to 2.82 g;
- the catalyst powder is shaped into a cylinder having an outer diameter (D) of 5.0 mm and a length (L) of 5.5 mm; Except that this was calcined for 5 hours under 460 ° C in an air atmosphere,
- the content of potassium nitrate is adjusted to 2.35 g;
- the catalyst powder is shaped into a cylinder having an outer diameter (D) of 4.0 mm and a length (L) of 4.5 mm; Except that this was calcined for 5 hours under 450 ° C in an air atmosphere,
- a cylindrical shell, three tube sheets separating the inside of the shell into two independent spaces, a baffle dividing the two independent spaces inside the shell into two spatially contiguous sections, the rib sheet and A shell-end-tube reaction vessel was prepared comprising a plurality of reaction tubes (inner diameter 1 inch, length 300 cm, stainless steel) secured inside the shell through a baffle.
- the reaction chamber the first fixed catalyst packed zone filled with the catalyst A by a length of 700 mm from the inlet; A second fixed catalyst bed zone in which the catalyst B is layered by a length of 700 mm; 13 fixed catalyst bed zone filled with the catalyst C by a length of 1000 mm; And a fourth fixed catalyst bed zone filled with the catalyst D by a length of 000 mm.
- first and second fixing Heat transfer to the catalyst bed zone was achieved.
- reaction pressure 1-3 atm under a space velocity of 120 hr 1 of propylene, 16 vol.% Oxygen, water vapor of 10 vol. 0/0, and 65 heunhap gas containing nitrogen in a volume% is was supplied, 300 ° Passed under C with a contact time of 2 seconds.
- a fourth fixed catalyst bed zone in which the catalyst D is filled by a length of 800 mm is set.
- a third fixed catalyst bed zone filled with the catalyst D by a length of 1600 mm was set;
- a second fixed catalyst bed zone filled with the catalyst D by a length of 2300 mm was set;
- the heat transfer is performed by the flow of the first heat medium for the length of the first fixed catalyst bed zone and the sieve 2 fixed catalyst bed zone by the length of 700 mm, and by the flow of the second heat medium for the rest of the second : fixed catalyst bed zone. Except for heat transfer,
- the temperature of the hot spot was measured in the gas phase contact oxidation reaction according to the above examples and comparative examples, and the conversion rate (%) of propylene, selectivity (%) for acrylic acid and acrolein, and yield (%) according to the following equations: ) was calculated.
- % Selectivity for acrylic acid (AA) and acrolein (ACR) [(moles of generated acrylic acid and acrolein) / (moles of reacted propylene)] * 100
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JP2018547443A JP6762370B2 (ja) | 2016-11-01 | 2017-10-17 | 不飽和アルデヒド及び不飽和カルボン酸の製造方法 |
US16/082,704 US10428007B2 (en) | 2016-11-01 | 2017-10-17 | Method for producing unsaturated aldehyde and unsaturated carboxylic acid |
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US20190092713A1 (en) | 2019-03-28 |
EP3415492B1 (en) | 2024-04-17 |
KR102084768B1 (ko) | 2020-03-04 |
CN109071393A (zh) | 2018-12-21 |
KR20180047836A (ko) | 2018-05-10 |
US10428007B2 (en) | 2019-10-01 |
JP6762370B2 (ja) | 2020-09-30 |
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EP3415492A1 (en) | 2018-12-19 |
CN109071393B (zh) | 2022-03-18 |
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