WO2020175373A1 - 青酸の製造方法及び青酸の製造装置 - Google Patents
青酸の製造方法及び青酸の製造装置 Download PDFInfo
- Publication number
- WO2020175373A1 WO2020175373A1 PCT/JP2020/007074 JP2020007074W WO2020175373A1 WO 2020175373 A1 WO2020175373 A1 WO 2020175373A1 JP 2020007074 W JP2020007074 W JP 2020007074W WO 2020175373 A1 WO2020175373 A1 WO 2020175373A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- hydrocyanic acid
- raw material
- bed reactor
- material gas
- fluidized bed
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/02—Preparation, separation or purification of hydrogen cyanide
- C01C3/0208—Preparation in gaseous phase
- C01C3/0241—Preparation in gaseous phase from alcohols or aldehydes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- 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
- B01J23/88—Molybdenum
- B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/8877—Vanadium, tantalum, niobium or polonium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/195—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium or tantalum
- B01J27/198—Vanadium
- B01J27/199—Vanadium with chromium, molybdenum, tungsten or polonium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/0025—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor by an ascending fluid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/02—Preparation, separation or purification of hydrogen cyanide
- C01C3/0208—Preparation in gaseous phase
- C01C3/0212—Preparation in gaseous phase from hydrocarbons and ammonia in the presence of oxygen, e.g. the Andrussow-process
- C01C3/0216—Preparation in gaseous phase from hydrocarbons and ammonia in the presence of oxygen, e.g. the Andrussow-process characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/02—Preparation, separation or purification of hydrogen cyanide
- C01C3/0208—Preparation in gaseous phase
- C01C3/0212—Preparation in gaseous phase from hydrocarbons and ammonia in the presence of oxygen, e.g. the Andrussow-process
- C01C3/022—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00539—Pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00911—Sparger-type feeding elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/0092—Perforated plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
Definitions
- the present invention relates to a method for producing hydrocyanic acid and an apparatus for producing hydrocyanic acid.
- Patent Document 1 describes that when a raw material such as methanol is subjected to ammoxidation in a fluidized bed reactor, the density of the fluid solid matter at the feed port of the raw material is Gas flow rate is 1
- the oxygen-containing gas is supplied from the supply port at the bottom thereof, and another supply port (gas disperser) at a predetermined position above the supply port of the oxygen-containing gas is provided. It is disclosed that the raw material is supplied from the open part).
- Patent Document 1 Japanese Patent Laid-Open No. 10-1 5 2 4 6 3
- the yield of hydrocyanic acid in the entire reactor may be low.
- An object of the present invention is to provide a process for producing hydrocyanic acid and a device for producing hydrocyanic acid, which can improve the yield of hydrocyanic acid in a gas-phase catalytic ammoxidation reaction of methanol.
- Patent Document 1 does not describe the number of openings of the gas disperser.
- the present invention has the following aspects.
- a raw material gas containing methanol is supplied into the fluidized bed reactor through a raw material gas disperser arranged in the fluidized bed reactor, and the methanol is mixed with ammonia and oxygen in the presence of a metal oxide catalyst.
- a gas phase catalytic ammoxidation reaction to obtain hydrocyanic acid
- the raw material gas disperser has one or more holes for discharging the raw material gas into the fluidized bed reactor, and the number of the holes per unit cross-sectional area of the fluidized bed reactor is 10 to 45. / ⁇ ! 2 , a method for producing hydrocyanic acid.
- the diameter of the hole is The method for producing hydrocyanic acid according to [1] or [2].
- the source gas disperser is a pipe type disperser
- a rectifying tube is attached to a position having the hole of the raw material gas disperser, and the raw material gas released from the hole is supplied into the fluidized bed reactor via the rectifying tube, [1] to [ [3] The method for producing hydrocyanic acid according to any one of [3].
- the source gas contains methanol and ammonia, [1] to [4 20/175373 3 ⁇ (: 170? 2020 /007074
- V, IV! ⁇ , ⁇ li, ⁇ , 3 I are iron, antimony, phosphorus, vanadium, molybdenum, copper, tungsten, oxygen, and silicon, respectively, and 8 is 1//19, 1.1 ⁇ % 1_ , 0 e s eight 1, ⁇ “, ⁇ ,
- Min. II and at least one element selected from the group consisting of 3 n
- Min represents at least one element selected from the group consisting of Min and Ding 6 ,
- 1 ⁇ /1 ⁇ , Minashi 6, ⁇ , 3 ⁇ are molybdenum, bismuth, ⁇ 2020/175 373 4 ⁇ (: 170? 2020 /007074
- IV and at least one element selected from the group consisting of 3 and IV! are 1_ and N 3, [ ⁇ , At least one selected from the group consisting of swallow and ⁇ 3.
- a device for producing hydrocyanic acid by contacting methanol with oxygen and oxygen in the presence of a metal oxide catalyst to produce a hydrocyanic acid by a vapor-phase catalytic ammoxidation reaction A fluidized bed reactor that performs an oxidation reaction
- One or more source gas dispersers disposed in the fluidized bed reactor
- a raw material gas supply unit for supplying a raw material gas containing methanol to the raw material gas disperser
- the raw material gas disperser has one or more holes for discharging the raw material gas into the fluidized bed reactor, and the number of the holes per unit cross-sectional area of the fluidized bed reactor is 10 to 45/ ⁇ ! 2 , a device for producing hydrocyanic acid. ⁇ 2020/175 373 5 ⁇ (: 170? 2020 /007074
- the yield of hydrocyanic acid in the vapor-phase catalytic ammoxidation reaction of methanol can be improved.
- FIG. 1 is a schematic configuration diagram of an apparatus for producing hydrocyanic acid according to an embodiment.
- Fig. 2 is a schematic top view of a raw material gas disperser to which a rectifying tube is attached, which is provided in the hydrogen cyanide production apparatus shown in Fig. 1.
- Fig. 3 is a cross-sectional view of the raw material gas disperser shown in Fig. 2.
- FIG. 4 is a graph showing the results of Examples 1 and 2 and Comparative Examples 1 and 2. MODE FOR CARRYING OUT THE INVENTION
- FIG. 1 is a schematic configuration diagram of an apparatus for producing hydrocyanic acid (hereinafter, also referred to as "present production apparatus") according to an embodiment of the present invention.
- FIG. 2 is a schematic top view of the raw material gas disperser 7 to which the rectifying pipe 8 is attached, which is included in the present manufacturing apparatus.
- FIG. 3 is a cross-sectional view of the raw material gas disperser shown in FIG.
- This production apparatus comprises a fluidized bed reactor 1 containing a particulate metal oxide catalyst 2 for performing a gas phase catalytic ammoxidation reaction, an oxygen-containing gas supply pipe 3 (oxygen-containing gas supply section), and an oxygen-containing gas supply unit.
- a gas disperser 4 a raw material gas supply pipe 6 (raw material gas supply unit), a raw material gas disperser 7, a rectifying pipe 8, a cyclone 9, a catalyst return pipe 10 and a gas discharge pipe 11 .
- the oxygen-containing gas disperser 4, the raw material gas disperser 7, the rectifying pipe 8, the cyclone 9, and the catalyst return pipe 10 are arranged in the fluidized bed reactor 1, respectively. ⁇ 2020/175373 6 ⁇ (: 170? 2020/007074
- the oxygen-containing gas supply pipe 3 is a pipe for supplying an oxygen-containing gas (for example, air) to the fluidized bed reactor 1.
- the oxygen-containing gas supply pipe 3 is connected to the bottom of the fluidized bed reactor 1.
- the raw material gas supply pipe 6 is a pipe for supplying a raw material gas containing methanol.
- the raw material gas supply pipe 6 is connected below the center of the fluidized bed reactor 1 in the height direction and communicates with the raw material gas disperser 7.
- the oxygen-containing gas disperser 4 is arranged above the connection position of the oxygen-containing gas supply pipe 3 of the fluidized bed reactor 1.
- the oxygen-containing gas disperser 4 divides the inside of the fluidized bed reactor 1 into upper and lower parts, and the metal oxide catalyst 2 is fluidly accommodated on the oxygen-containing gas disperser 4.
- the raw material gas disperser 7 is arranged below the center of the fluidized bed reactor 1 in the height direction and above the oxygen-containing gas disperser 4.
- the height of the raw material gas disperser 7 may be any position. Two or more raw material gas dispersers 7 may be arranged so that the raw material gas is divided and supplied.
- the straightening tube 8 is attached to the raw material gas disperser 7.
- the cyclone 9 is arranged near the top of the fluidized bed reactor 1.
- the first end of the catalyst return pipe 10 is connected to the cyclone 9.
- the second end opposite to the first end can be opened at any position, for example, it can be opened between the oxygen-containing gas distributor 4 and the raw material gas distributor 7.
- a flapper valve or a trickle valve may be installed at the opening of the catalyst return pipe 10.
- the gas discharge pipe 11 is a pipe for discharging gas from the fluidized bed reactor 1.
- the gas discharge pipe 11 is connected to the top of the fluidized bed reactor 1 and communicates with the cyclone 9.
- the cyclone 9 may be a series multi-stage cyclone in which two or more cyclones are connected in series.
- the gas discharge pipe 11 communicates with the last cyclone of the cyclones forming the series multi-stage cyclone.
- the metal oxide catalyst 2 is a gas phase contact catalyst of methanol in a fluidized bed reactor. ⁇ 2020/175 373 7 ⁇ (: 170? 2020 /007074
- the average particle size of the metal oxide catalyst 2 is preferably 30 to 200.
- the lower limit of the average particle size is more preferably 40 or more, and the upper limit is more preferably 100 or less.
- the lower limit of bulk density is ⁇ . More preferably, the upper limit is 1. The following are more preferable.
- the metal oxide catalyst 2 preferably has high activity.
- a highly active catalyst having a reaction rate constant of 33 ⁇ 1 or more when the ammoxidation reaction is the first-order reaction of methanol, which is an index of activity, is preferable.
- a preferable example of the metal oxide catalyst 2 is a metal oxide catalyst containing at least iron, antimony, phosphorus and vanadium. Such a metal oxide catalyst is excellent in terms of reaction rate and resistance to reduction deterioration.
- Metal oxide catalysts containing at least iron, antimony, phosphorus, and vanadium have a high yield of prussic acid, a high selectivity, and a stable yield over time even when the concentration of methanol is high.
- the number of moles of iron in the metal oxide catalyst is 10
- the number of moles of vanadium is preferably 0.6 or more, and more preferably the composition represented by the following formula (I).
- V, IV! ⁇ , ⁇ ri, ⁇ , 3 I are iron, antimony, phosphorus, vanadium, molybdenum, copper, tungsten, oxygen, and silicon, and 8 is 1 ⁇ /19, 1.1 ⁇ % 1_ , 0 e s eight 1, ⁇ “, ⁇ ,
- Min. II and at least one element selected from the group consisting of 3 n
- Min represents at least one element selected from the group consisting of Min and Ding 6 ,
- the metal oxide catalyst 2 is a metal oxide catalyst containing at least molybdenum and bismuth. Such a metal oxide catalyst is excellent in terms of reaction rate and resistance to reduction deterioration.
- the metal oxide catalyst containing at least molybdenum and bismuth has the following formula ( ⁇ ) from the viewpoint that even if the concentration of methanol is increased, hydrocyanic acid can be obtained with high yield, high selectivity and stable with time. It is more preferable to have a composition represented by
- 6, 6, 0 and 3 are respectively molybdenum, bismuth, iron, oxygen and silicon, and'' is at least 1 ⁇ 1 and IV! 9, 1 ⁇ / ⁇ and at least one selected from the group consisting of Indicates a kind of element, 1_ is 1_3, ⁇ 6,
- IV and at least one element selected from the group consisting of 3 and IV! are 1_ and N 3, [ ⁇ ,
- oxygen-containing gas disperser 4 a known disperser can be used, and examples thereof include pipe type including pipe grid type, cap type, porous plate type, perforated plate type and parallel slit plate type.
- a pipe type disperser including a pipe grid type is used as the source gas disperser 7. ⁇ 2020/175 373 9 (: 170? 2020/007074
- An example of the raw material gas disperser 7 is, as shown in FIG. 2, a header 71 extending in a first direction (horizontal direction in FIG. 2) and a second direction (vertical direction) extending from the header 71 to the first direction. (Up-down direction in Fig. 2)
- This is a pipe-type distributor including a plurality of branch pipes 72 extending on both sides.
- the header 7 1 communicates with the raw material gas supply pipe 6, and the branch pipe 7 2 communicates with the header _ 7 1.
- the branch pipe 72 is formed with a hole 73 that opens toward the lower side when the raw material gas disperser 7 is arranged in the fluidized bed reactor 1.
- the header 71 may be provided with a hole 73 that opens toward the lower side when the raw material gas disperser 7 is arranged in the fluidized bed reactor 1.
- the branch pipe 72 may not be provided.
- the number of holes 73 per unit cross-sectional area of the fluidized bed reactor 1 (hereinafter, also referred to as "the number of holes per unit reactor cross-sectional area") is 10 to 45 / 2 , 20 to 35 pieces/0! 2 are preferable.
- the number of pores per unit reactor cross-sectional area is within the above range, the yield of hydrocyanic acid in the gas-phase catalytic ammoxidation reaction of methanol is excellent.
- the number of holes per unit reactor cross-sectional area is calculated by dividing the number (holes) of the holes 73 in the raw material gas disperser 7 by the cross-sectional area ( 2 ) of the fluidized bed reactor 1.
- the number of holes per unit reactor cross-sectional area can be changed, for example, by changing the number of branch pipes 7 2 or by changing the number of holes 7 3 formed in the header 7 1 or one branch pipe 7 2. It can be adjusted.
- the branch pipes 72 and the holes 73 are preferably provided at uniform intervals.
- the cross-sectional area of the fluidized bed reactor 1 refers to the area of the cross section inside the fluidized bed reactor 1 at the height where the raw material gas distributor 7 is arranged in the fluidized bed reactor 1.
- the cross section is a cross section in a direction orthogonal to the height direction.
- the cross-sectional area includes the cross-sectional area of the interior of the catalyst return pipe 10 and the like.
- the area obtained by subtracting the cross-sectional area of the interior from the cross-sectional area of the fluidized bed reactor 1 is the effective cross section of the fluidized bed reactor. ⁇ 2020/175 373 10 ⁇ (: 170? 2020 /007074
- Sectional area of the fluidized bed reactor may be suitable Yichun selected in the range of 1 0 X 1 0 _ 2 ⁇ 1 5_Rei 2.
- the ratio of the area of the holes 73 to the cross-sectional area of the fluidized bed reactor 1 is preferably 0.01 to 0.2 area%, and the lower limit is It is more preferably 0.03 area% or more, and the upper limit is more preferably 0.1 area% or less.
- the diameter of holes 7 3 is 1 to 12 Is preferable from the viewpoint of the yield of hydrocyanic acid.
- the lower limit of the diameter of hole 73 is 1. The above is more preferable, and the upper limit is 8 The following is more preferable.
- the pressure loss in the disperser is in an appropriate range, which is advantageous in terms of power cost for supplying the raw material gas and uniform dispersibility of the raw material gas.
- the diameters of the plurality of holes 73 may be the same or different.
- the rectifying pipe 8 is attached to a position of the hole 7 3 on the outer peripheral surface of the branch pipe 7 2 and communicates with the branch pipe 72.
- the rectifying pipe 8 is attached to the position of the hole 7 3 on the outer peripheral surface of the header 7 1 and communicates with the header 7 1.
- the inner diameter of the straightening pipe 8 is, for example, more than the diameter of the hole 73,
- the length of the rectifying tube 8 is, for example, Is.
- Production of hydrocyanic acid using the present production apparatus can be carried out, for example, by the following procedure.
- the oxygen-containing gas is supplied from the oxygen-containing gas supply pipe 3 to the bottom of the fluidized bed reactor 1. At this time, the supplied oxygen-containing gas is supplied upward through the oxygen-containing gas disperser 4, and the metal oxide catalyst 2 is brought into a fluidized state to form a fluidized bed.
- the supplied raw material gas is introduced into the branch pipe 7 2 via the header 71, and is discharged from the hole 73 to the lower side of the raw material gas disperser 7. Further, the raw material gas discharged from the hole 73 is supplied into the fluidized bed reactor 1 via the straightening pipe 8. Specifically, the raw material gas discharged from the hole 73 is blown out from the tip of the rectifying tube 8 toward the lower part of the raw material gas disperser 7, and then, while contacting with the metal oxide catalyst 2 in a fluid state. Ascend in the fluidized bed reactor 1. During this period, methanol in the raw material gas comes into contact with ammonia in the raw material gas and oxygen in the oxygen-containing gas, and hydrocyanic acid (hydrogen cyanide) is produced by the vapor-phase contact ammoxidation reaction.
- hydrocyanic acid hydrocyanic acid
- the generated reaction gas containing hydrocyanic acid is introduced into the cyclone 9 together with the metal oxide catalyst 2 entrained in the gas stream.
- the reaction gas and the metal oxide catalyst 2 are separated.
- the metal oxide catalyst 2 separated by the cyclone 9 is returned to the fluidized bed reactor 1 through the catalyst return pipe 10 and the reaction gas is passed from the cyclone 9 through the gas discharge pipe 11 to the fluidized bed reactor 1 Discharged from.
- Air is usually used as the oxygen-containing gas.
- oxygen-containing gas oxygen-enriched air or oxygen gas diluted with an inert gas may be used.
- the source gas may contain a diluent such as nitrogen, carbon dioxide or water vapor in addition to methanol and ammonia.
- the temperature at which methanol is brought into contact with ammonia and oxygen is preferably 300 to 500°C from the viewpoint of the yield of hydrocyanic acid.
- the lower limit of the temperature is more preferably 3 5 0 ° ⁇ As, more preferably 3 8 0 ° ⁇ As. Further, the upper limit is more preferably 470 ° or less. This temperature is determined by measuring the temperature in the fluidized bed reactor. The measurement point may be, for example, a portion above the position (height) of the raw material gas disperser where the reaction with the metal oxide catalyst occurs.
- the pressure is 0 to 200. 3 is preferred. Lower pressure limit is 10 3 or more is more preferable, and the upper limit is 150 3 or less is more preferable.
- the pressure is a gauge pressure. This pressure is determined by measuring the pressure at the top of the fluidized bed reactor.
- the molar ratio of oxygen to methanol is preferably from 0.8 to 2.0, and more preferably from 0.8 to 1.5, from the viewpoint of the yield of hydrocyanic acid.
- oxygen/methanol oxygen/methanol
- the molar ratio of air to methanol is 3.
- It is preferably 8 to 9.5, and more preferably 3.8 to 7.1.
- the molar ratio of ammonia to methanol is preferably 0.5 to 10 from the viewpoint of the yield of hydrocyanic acid.
- the superficial velocity of all the supplied gases is 10 to 200 from the viewpoint of the yield of hydrocyanic acid.
- the lower limit of the superficial velocity of all the supplied gas is more preferably 200 01/36° or more, and the upper limit is The following is more preferable.
- the superficial velocity of methanol and the superficial velocity of ammonia are both preferably 1 to 300, 01/360.
- the lower limit of the superficial velocity of methanol and the lower limit of the superficial velocity of ammonia are both preferably 200 1/360 or more, and more preferably 20001/36 60 or less.
- the superficial velocity of oxygen is preferably 2 to 4200 01/360.
- the lower limit of the superficial velocity of oxygen is more preferably 40111/360 or more, and the upper limit is more preferably 210111/360 or less.
- the superficial velocity of air is preferably 10 to 200 00 01/360.
- the lower limit of the superficial velocity of air is more preferably 20 cm x 360 or more, and the upper limit is more preferably 100 000 /360 or less.
- the definition of the superficial velocity is as described in Examples described later.
- the yield of hydrocyanic acid can be improved.
- the distribution of methanol in the fluidized bed reactor 1 will be non-uniform. Due to the non-uniform distribution of methanol, there is a region in the fluidized bed reactor 1 in which oxygen is relatively deficient with respect to methanol and a large amount of methanol remains unreacted. On the other hand, there is a region in which a relatively large amount of by-products are formed and a large amount of by-products are generated, and the yield of hydrocyanic acid in the entire fluidized bed reactor is reduced.
- the distribution state of methanol in the fluidized bed reactor 1 is made uniform, and the contact between the source gas and the metal oxide catalyst 2 is also improved. It is considered that the condition can be improved and the yield of hydrocyanic acid is improved.
- the raw material gas can be rectified and the flow rate of the raw material gas is reduced to prevent metal flow. It is possible to prevent the particles of the oxide catalyst from being pulverized.
- per unit reactor cross-sectional area for improving the yield The optimum value of the number of holes is different.
- a pipe-type disperser is used as the raw material gas disperser 7
- the raw material gas disperser 7 can have the number of holes per unit reactor cross-sectional area within the above range.
- Any known disperser other than the pipe-type disperser may be used.
- a disperser other than the pipe disperser for example, a cap ⁇ 2020/175 373 14 ⁇ (: 170? 2020 /007074
- the mold examples include a porous plate type, a porous plate type, and a parallel slit plate type.
- a pipe type disperser is preferable because it is excellent in that clogging of the catalyst can be suppressed and the structure is simple.
- a raw material gas containing ammonia was used together with methanol, which is the target (raw material) of vapor phase catalytic ammoxidation, and methanol and ammonia were supplied to the fluidized bed reactor 1 all at once.
- methanol and ammonia may be supplied separately.
- a gas supply pipe for an ammonia-containing gas and a gas disperser may be provided to supply the ammonia-containing gas into the fluidized bed reactor 1 in addition to methanol.
- a raw material gas containing methanol and ammonia is preferably used from the viewpoint that methanol and ammonia can be reliably mixed.
- the oxygen-containing gas may be supplied into the fluidized bed reactor 1, for example, by providing a gas supply pipe and a gas disperser for the oxygen-containing gas other than the bottom of the fluidized bed reactor 1. From the viewpoint of fluidizing the metal oxide catalyst 2, it is preferable to supply the oxygen-containing gas from the bottom of the fluidized bed reactor 1.
- a cooling pipe may be provided in the fluidized bed reactor 1.
- the temperature in the fluidized bed reactor 1 can be easily controlled within the optimum temperature range for the gas phase catalytic ammoxidation reaction. Therefore, the raw material gas containing a high concentration of methanol can be processed, and the productivity is improved.
- Examples of the cooling pipe include a vertical cooling pipe, a horizontal cooling pipe, and a spiral cooling pipe.
- the effective area of the fluidized bed reactor means the sectional area of the interior of the catalyst return pipe 10 etc. from the sectional area of the part where the reaction between the raw material gas and the metal oxide catalyst 2 occurs in the fluidized bed reactor 1. The reduced area is shown.
- Antimony trioxide powder 247.3 was weighed out.
- Nitric acid 385 !_ and water 480 !_ were mixed and heated, and electrolytic iron powder 49.99 was added little by little and dissolved therein. Then, to this solution, copper nitrate 54.09 was added and dissolved.
- silica sol (3 ⁇ 2:20 wt%) was weighed 1 5909.
- Table 1 shows the conditions for gas phase catalytic ammoxidation reaction of methanol in Example 1.
- ⁇ in “3 ⁇ ” indicates gauge pressure (the same applies below).
- the fluidized bed reactor 1 was filled with 60! ⁇ 9 of the catalyst (_ 1), air was supplied from the oxygen-containing gas supply pipe 3, and the mixture of methanol and ammonia was supplied from the raw material gas supply pipe 6. Gas (raw material gas) was supplied to carry out the reaction. At this time, the molar ratio of oxygen/methanol in the air is 1.4 (the molar ratio of air/methanol is 6.5), the molar ratio of ammonia/methanol is 1, and the superficial velocity of all the supplied gases is 5
- Example 2 After the reaction of Example 1 was changed from the temperature only 4 3 0 ° ⁇ to 4 3 9 ° ⁇ . After the temperature was changed, it was confirmed that the reaction gas composition was stable, and the yield of hydrocyanic acid was calculated from the measurement result of the reaction gas composition at this time, which was used as the first reaction (re n 1). Then, in order to confirm the reproducibility, the reaction gas composition was measured again to calculate the cyanide yield, which was used as the second reaction (“ n 2 ). The cyanide yield in Example 2 is also shown in Table 1.
- the hydrocyanic acid was prepared in the same manner as in Example 1 except that the manufacturing conditions were changed as shown in Table 1. ⁇ 2020/175 373 17 ⁇ (: 170? 2020 /007074
- Fig. 4 shows the relationship between the number of holes per unit reactor cross-sectional area and hydrocyanic acid yield in Examples 1 and 2 and Comparative Examples 1 and 2, respectively.
- Example 1 As can be seen from Table 1, the reaction conditions of Example 1 and Comparative Example 1, and Example 2 ⁇ 2020/175 373 18 ⁇ (: 170? 2020 /007074
- the number of holes per unit reactor cross-section is 10 ⁇
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
KR1020217008735A KR102602678B1 (ko) | 2019-02-27 | 2020-02-21 | 시안화수소산의 제조 방법 및 시안화수소산의 제조 장치 |
JP2021502192A JP7294401B2 (ja) | 2019-02-27 | 2020-02-21 | 青酸の製造方法及び青酸の製造装置 |
US17/221,387 US20210238049A1 (en) | 2019-02-27 | 2021-04-02 | Method for Producing Hydrocyanic Acid and Device for Producing Hydrocyanic Acid |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2019-034279 | 2019-02-27 | ||
JP2019034279 | 2019-02-27 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/221,387 Continuation US20210238049A1 (en) | 2019-02-27 | 2021-04-02 | Method for Producing Hydrocyanic Acid and Device for Producing Hydrocyanic Acid |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2020175373A1 true WO2020175373A1 (ja) | 2020-09-03 |
Family
ID=72239564
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2020/007074 WO2020175373A1 (ja) | 2019-02-27 | 2020-02-21 | 青酸の製造方法及び青酸の製造装置 |
Country Status (4)
Country | Link |
---|---|
US (1) | US20210238049A1 (ja) |
JP (1) | JP7294401B2 (ja) |
KR (1) | KR102602678B1 (ja) |
WO (1) | WO2020175373A1 (ja) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN116242545B (zh) * | 2023-05-10 | 2023-07-14 | 山东宏旭化学股份有限公司 | 一种氢氰酸氧化反应器的安全检测装置及其使用方法 |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS58145617A (ja) * | 1982-02-22 | 1983-08-30 | Nitto Chem Ind Co Ltd | シアン化水素の製造法 |
JPH01171640A (ja) * | 1987-12-25 | 1989-07-06 | Nitto Chem Ind Co Ltd | 流動層反応に適する鉄・アンチモン・リン含有触媒の製法 |
JPH01257125A (ja) * | 1988-04-05 | 1989-10-13 | Nitto Chem Ind Co Ltd | 青酸製法 |
JPH10152463A (ja) * | 1996-09-25 | 1998-06-09 | Nitto Chem Ind Co Ltd | 流動層反応器におけるアンモ酸化法 |
JP2002097017A (ja) * | 2000-09-21 | 2002-04-02 | Mitsubishi Rayon Co Ltd | シアン化水素の製造方法 |
JP2007063089A (ja) * | 2005-09-01 | 2007-03-15 | Mitsubishi Rayon Co Ltd | ニトリル化合物の製造方法および製造装置 |
JP2008043894A (ja) * | 2006-08-18 | 2008-02-28 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1426254A (en) * | 1972-10-06 | 1976-02-25 | Sumitomo Chemical Co | Process for preparing hydrogen cyanide |
EP0832877B1 (en) * | 1996-09-25 | 2001-11-21 | Mitsubishi Rayon Co., Ltd. | Ammoxidation method in fluidized-bed reactor |
JP3506872B2 (ja) * | 1997-03-13 | 2004-03-15 | 三菱レイヨン株式会社 | 青酸の製造方法 |
-
2020
- 2020-02-21 WO PCT/JP2020/007074 patent/WO2020175373A1/ja active Application Filing
- 2020-02-21 KR KR1020217008735A patent/KR102602678B1/ko active IP Right Grant
- 2020-02-21 JP JP2021502192A patent/JP7294401B2/ja active Active
-
2021
- 2021-04-02 US US17/221,387 patent/US20210238049A1/en active Pending
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS58145617A (ja) * | 1982-02-22 | 1983-08-30 | Nitto Chem Ind Co Ltd | シアン化水素の製造法 |
JPH01171640A (ja) * | 1987-12-25 | 1989-07-06 | Nitto Chem Ind Co Ltd | 流動層反応に適する鉄・アンチモン・リン含有触媒の製法 |
JPH01257125A (ja) * | 1988-04-05 | 1989-10-13 | Nitto Chem Ind Co Ltd | 青酸製法 |
JPH10152463A (ja) * | 1996-09-25 | 1998-06-09 | Nitto Chem Ind Co Ltd | 流動層反応器におけるアンモ酸化法 |
JP2002097017A (ja) * | 2000-09-21 | 2002-04-02 | Mitsubishi Rayon Co Ltd | シアン化水素の製造方法 |
JP2007063089A (ja) * | 2005-09-01 | 2007-03-15 | Mitsubishi Rayon Co Ltd | ニトリル化合物の製造方法および製造装置 |
JP2008043894A (ja) * | 2006-08-18 | 2008-02-28 | Asahi Kasei Chemicals Corp | 流動層反応器の温度制御方法 |
Also Published As
Publication number | Publication date |
---|---|
KR102602678B1 (ko) | 2023-11-16 |
US20210238049A1 (en) | 2021-08-05 |
JP7294401B2 (ja) | 2023-06-20 |
KR20210044876A (ko) | 2021-04-23 |
JPWO2020175373A1 (ja) | 2021-09-30 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US8517180B2 (en) | Process for charging a reactor with a fixed catalyst bed which comprises at least annular shaped catalyst bodies K | |
TWI450765B (zh) | 將自環狀經塗覆觸媒k之至少一種生產加料取出的部份導入管束反應器之反應管中之方法 | |
JP5106765B2 (ja) | ニトリル化合物の製造方法および製造装置 | |
CN108940137B (zh) | 流化床反应装置及α,β-不饱和腈的制造方法 | |
WO2020175373A1 (ja) | 青酸の製造方法及び青酸の製造装置 | |
CN110256286B (zh) | 化合物的制造方法 | |
WO2016147950A1 (ja) | 流動床反応器に触媒を充填する方法及びニトリル化合物の製造方法 | |
KR102000899B1 (ko) | 불포화 니트릴의 제조 방법 | |
US5965765A (en) | Process for producing α,β-unsaturated nitrile | |
JP7352692B2 (ja) | 不飽和ニトリルの製造方法 | |
JP6427723B1 (ja) | 不飽和ニトリルの製造方法 | |
EP3431175A1 (en) | Method of reaction with heat-exchange-type reactor and method of packing packing material into plate-type reactor | |
RU2732413C1 (ru) | Способ получения ненасыщенного нитрила | |
JP2020083832A (ja) | 不飽和ニトリルの製造方法 | |
TWI685380B (zh) | 不飽和腈之製造方法 | |
JP2020200274A (ja) | アクリロニトリルの製造方法 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 20762594 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2021502192 Country of ref document: JP Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 20217008735 Country of ref document: KR Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 20762594 Country of ref document: EP Kind code of ref document: A1 |