GB2229173A - Production of hydrogen peroxide by anthraquinone process - Google Patents
Production of hydrogen peroxide by anthraquinone process Download PDFInfo
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- GB2229173A GB2229173A GB9001802A GB9001802A GB2229173A GB 2229173 A GB2229173 A GB 2229173A GB 9001802 A GB9001802 A GB 9001802A GB 9001802 A GB9001802 A GB 9001802A GB 2229173 A GB2229173 A GB 2229173A
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- United Kingdom
- Prior art keywords
- hydrogen
- static mixer
- static
- mixing zone
- working solution
- Prior art date
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- 238000000034 method Methods 0.000 title claims description 34
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims description 30
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 title claims description 13
- 150000004056 anthraquinones Chemical class 0.000 title claims description 13
- 238000004519 manufacturing process Methods 0.000 title claims description 5
- 239000012224 working solution Substances 0.000 claims description 39
- 230000003068 static effect Effects 0.000 claims description 37
- 229910052739 hydrogen Inorganic materials 0.000 claims description 31
- 239000001257 hydrogen Substances 0.000 claims description 31
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 29
- 239000007789 gas Substances 0.000 claims description 22
- 238000002156 mixing Methods 0.000 claims description 21
- 239000011541 reaction mixture Substances 0.000 claims description 15
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 13
- 229910052751 metal Inorganic materials 0.000 claims description 10
- 239000002184 metal Substances 0.000 claims description 10
- RZVHIXYEVGDQDX-UHFFFAOYSA-N 9,10-anthraquinone Chemical compound C1=CC=C2C(=O)C3=CC=CC=C3C(=O)C2=C1 RZVHIXYEVGDQDX-UHFFFAOYSA-N 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 8
- 239000003960 organic solvent Substances 0.000 claims description 7
- 229910052763 palladium Inorganic materials 0.000 claims description 6
- 239000011949 solid catalyst Substances 0.000 claims description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 4
- 239000011248 coating agent Substances 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- 229910052703 rhodium Inorganic materials 0.000 claims description 2
- 239000010948 rhodium Substances 0.000 claims description 2
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 2
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims 1
- 239000000377 silicon dioxide Substances 0.000 claims 1
- 239000003054 catalyst Substances 0.000 description 34
- 238000005984 hydrogenation reaction Methods 0.000 description 26
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 7
- 241000264877 Hippospongia communis Species 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000008188 pellet Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000010517 secondary reaction Methods 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 230000001419 dependent effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- SJEBAWHUJDUKQK-UHFFFAOYSA-N 2-ethylanthraquinone Chemical compound C1=CC=C2C(=O)C3=CC(CC)=CC=C3C(=O)C2=C1 SJEBAWHUJDUKQK-UHFFFAOYSA-N 0.000 description 1
- PCFMUWBCZZUMRX-UHFFFAOYSA-N 9,10-Dihydroxyanthracene Chemical class C1=CC=C2C(O)=C(C=CC=C3)C3=C(O)C2=C1 PCFMUWBCZZUMRX-UHFFFAOYSA-N 0.000 description 1
- 239000007868 Raney catalyst Substances 0.000 description 1
- 229910000564 Raney nickel Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 150000002903 organophosphorus compounds Chemical class 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
- C01B15/01—Hydrogen peroxide
- C01B15/022—Preparation from organic compounds
- C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2435—Loop-type reactors
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00094—Jackets
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
- B01J2219/324—Composition or microstructure of the elements
- B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Description
!1 A PROCESS FOR THE PREPARATION OF HYDROGEN PEROXIDE The present
invention relates to a process for preparation of hydrogen peroxide by the anthraquinone process, and more particularly to a part of the process, namely the hydrogenation. Quite specifically the present invention relates to a process in which a reaction solution is circulated into which hydrogen or a hydrogen-containing gas and a working solution, i.e. an anthraquinone derivative in an organic solvent, are fed via a tubular static mixing zone which is either continuous or made up of several parts, in order to hydrogenate the anthraquinone derivative in the presence of a solid catalyst and by removing hydrogenated working solution and gas from the circulating reaction mixture. In addition the present invention relates to a tubular static mixer comprising one or more parts and to the use of the mixer in the process mentioned above.
It is known that hydrogen peroxide can be prepared by the so-called anthraquinone process. In this process an anthraquinone derivative is dissolved in a solvent comprising one or more components. The solution thus prepared is called the working solution.
In the preparation of hydrogen peroxide, the working solution is first fed to the hydrogenation step.
Durin g this step the anthraquinone derivatives are hydrogenated, in the presence of a catalyst, to the corresponding anthrahydroquinone derivatives.
Thereafter the hydrogenated working solutions directed to oxidation, during which oxygen or an oxygen containing gas is introduced into it, whereupon hydrogen peroxide is formed in the solution. The principal reactions of the anthraquinone process are cl t 1 2 shown below:
0 + N2 0 OH @4C__R ON 011 1 R catalyst > WOO) 1 off 0 + 02 -> R 0 0 + 11202 0 The working solution which contains hydrogen peroxide is fed to the extraction step, in which the hydrogen peroxide is caused by extraction to pass from the working solution into an aqueous solution. The extracted working solution is derived by removal of excess water and recycled to the beginning of the cyclic process, i.e. to hydrogenation. The aqueous solution of hydrogen peroxide, obtained by extraction, is purified and concentrated.
The hydrogenation described above is a demanding step in the anthraquinone process. High activity and high selectivity are required of the hydrogenation catalyst. The conversion and selectivity of the reaction in the hydrogenation step are dependent on the partial pressure of hydrogen, the temperature, the concentrations of the reacting components, the t 3 catalyst, and the flow conditions in the reactor. Secondary reactions may decrease the quantity of the anthraquinone derivatives which produce hydrogen peroxide. Both suspension reactors and fixed-bed reactors have been used for the hydrogenation.
The suspended catalysts used have included porous so-called palladium black, palladium absorbed into a carrier (for example alumina, activated carbon), and Raney nickel. The porous catalyst is suspendec?,and the hydrogen is dispersed into the working solution in, for example, a mixingtank reactor or a tubular reactor. In a tubular reactor the mixing is effected by the high linear velocity of the working solution. Usually, the linear velocities are over 3 m/s and below 10 mls in an open tube (US Patent 4,428,923). Mixing has also been improved by using as a reactor tube an alternately converging and expanding tube (US Patent 3,423,176, Kabisch et al).
From FI Patent Application 864 971 there is additionally known a process of the type mentioned in the preamble, in which a reaction mixture which contains hydrogen, working solution and a solid suspended catalyst is circulated in a tubular reactor system which is equipped with a static mixer which is continuous or made up of several parts. The pressure prevailing in the tube system is below 15 bar and the temperature below 1000C. In this process the working solution is circulated in the reaction tube system at flow velocity which is below 3 m/s.
a The contact surfaces and contact periods of the catalyst, the working solution and the hydrogen gas are important for the hydrogenation reaction. By using a 4 stationary, solid catalyst in the hydrogenation the contact period in the catalyst reaction can be shortened, whereby the proportion of secondary reactions is decreased. The absence of the expensive filtration step is a significant advantage of using a fixed catalyst bed rather than a suspended catalyst. The filtration may be problematic also technically, since the catalyst particles are small.
A suspended catalyst is left partly unexploited in the hydrogenation reaction, since for a large proportion of the time it is in a hydrogenfree part of the process cycle, for example in the circulation tank, or it may adhere to the process cycle. Also, a suspended catalyst is more sensitive to sintering and to mechanical wear.
In fixed-bed reactors, carrier pellets and so- called honey-comb catalysts have been used (Berglin et al., US Patent 4,552,748). The carrier used has usually been active alumina, but also other porous carrier having a large specific surface can be used, for example Si02 or activated carbon. A noble metal, usually palladium, has been absorbed as the active component into the carrier. only some kind of after filtra'tion for the separation, from the working solution, of particles detached from the bed is used in the fixed-bed reactor before the oxidation step.
In fixed-bed reactors there are usually used pellets (diameter usually 0. 2-10 mm) installed between sieve sheets or nets. In pellets as large as this, the transfer of material into the deepest pores and out of them is slow, for which reason the active metal in the inner parts of the pellets remains unexploited in the reaction. Likewise, the pressure loss increases to a high level, and canalization of the flows occurs in these freely packed catalyst beds. The reduction gas also tends to separate into a phase of its own, whereupon the hydrogenation velocity decreases. Special attention must be paid in order that no catalytic poisons will pass into the working solution or into the reduction gas.
The so-called honeycomb catalyst is made up of a cellular support structure having parallel canals. The porous carrier is fixed as a thin layer on the support structure, and furthermore a noble metal is absorbed into it. A reactor working according to a principle is such as this has the disadvantage of a poor mixing of the hydrogen with the working solution and possibly the separation of the gas bubbles into a phase of their own. Heat transfer from the inner parts of the honeycomb remains poor, in which case the temperature therein may rise too high, a situation which increases the quantity of undesirable byproducts.
It, one step limiting hydrogenation in fix-ed-bed reactors is the passage of hydrogen from a gas bubble into the working solution. The rate of the passage of hydrogen depends on the size of the hydrogen bubbles in the working solution. The smaller the bubbles in which the hydrogen is in the solution, the greater the total surface area of the interface between the working solution and the gas phase. The mixing of hydrogen with the working solution has been improved by using static mixers at a point before the fixed-bed reactor (US Patent 4,428,922). In this manner the hydrogen is in small bubbles in the working solution upon entering the reactor, but as a result of the canalization in the k 6 reactor the dispersion of the gas weakens.
A pre-mixing reactor in which the working solution is saturated with respect to hydrogen has also been used at a point before the hydrogenation (US Patent 2,837,411).
The purpose of the present invention is thus to provide a process and an apparatus for the production of hydrogen peroxide by the anthraquinone process, in which the disadvantage of prior-art processes and apparatuses have been eliminated.
According to the invention, there is provided a process for the production of hydrogen peroxide by the anthraquinone process by circulating a reaction mixture into which there are fed hydrogen or a hydrogencontaining gas and a working solution, comprising an anthraquinone derivative in an organic solvent, via a static mixing zone, in order to hydrogenate the anthraquinone derivative in the presence of a solid catalyst, and by removing hydrogenated working solution and gas from the circulating reaction mixture, in which process the reaction mixture is mixed, while it is being catalyzed, by circulating the reaction mixture via a'catalyst-coated static mixing zone.
The static mixing zone may be oblong and may be tl5 continuous or made up of several parts.
The invention also extends to a tubular static mixer, comprising one or several parts, for the catalytic hydrogenation of a reaction mixture which contains hydrogen or a hydrogen-containing gas and a working solution compriLing an anthraquinone derivative 1 7 in an.organic solvent, the static mixer being coated with a solid catalyst.
The invention also encompasses the use of a tubular static mixer, comprising one or several parts, for the catalytic hydrogenation of an anthraquinone derivative in an organic solvent by means of hydrogen or a hydrogen-containing gas, the surface of the static mixer having been coated with a porous carrier layer, preferably at maximum 300-um-thick, into which a hydrogenation-catalyzing metal has been absorbed.
In the process according to the invention, a reaction mixture comprising hydrogen or a hydrogencontaining gas and the working solution is thus caused to circulate in a constant-diameter or alternately converging and expanding tubular reactor system which is installed horizontally or vertically and is equipped with a static mixer which is continuous or comprises several parts and is coated with a catalytic substance, the reaction mixture being simultaneously mixed and catalyzed in the mixer. The tubular reactor can simply be dimensioned to be so long that the hydrogen has time to react before reaching the end of the tubular reactor. Thus reduction gas need not be circulated in the reactor.
The static mixer according to the invention comprises a support structure of a metallic, ceramic, po lymeric or other corresponding material, to the surface of which a porous carrier has been fixed. The carrier comprises, for example, alumina, Si02 t silicates or activated carbon. A metal active-in hydrogenation, for example palladium, platinum, rhodium, nickel or a mixture of these, has been t 8 absorbed into the carrier.
is C^ In the reactor according to the invention, a sufficient transfer of material between the gas and the liquid and a sufficient transfer of heat from the reactor mixture to the tube wall are achieved by means of static mixers, which have been described in the following publications, for example: Chem.-Ing.-Tech. 52 (1980), 4, pp. 285-291; Chem. Eng. Prog. 82 (July 1986), 7, pp. 42-48, and 20 (May-June 1986), 3, pp. 147-154; Perry, R.H. and Chilton, C.H., Chemical Engineer's Handbook, 5, New York: McGrawHill (1973) Section 19, p. 22 Likewise, axial mixing is minimised and the temperature and concentration profiles in the cross sectional area of the tube are made even.
The reaction occurs in a thin catalyst layer of preferably 5-300 um on the surface of the mixer. The layer being thin, the proportion of yielddecreasing secondary reactions will remain small, since the retention times of reagents and reaction products in the pores are short. Likewise, the catalytically active metal will be used efficiently in the thin catalyst layer. For this reason the catalyst layer according to the invention is more advantageous than a fixed bed made up of pellets.
In contrast to the honeycomb reactor according to US Patent 4,552,748, in which the catalyst pieces from mutually parallel, equally long canals with no mixing effect, in the reactor according to the invention its structures serve not only as fixing surfaces for the catalyst but also as mixers, the static mixer preferably having catalyst-coated flow baffles mutually in different directions, which effectively distribute 1 1 9 the flow over the entire cross sectional area of the reactor. Such an effect is not present in the reactor according to US Patent 4,552,748, which requires separate mixers for dispersing and dissolving the hydrogen into the working solution.
In the present invention it is quite essential that the reaction solution is mixed while it is being catalyzed, since it has been observed that hydrogenation reaction is not as effective if the catalyzing and the mixing are carried out in different steps, as in US Patent 4,552,748.
Owing to the mixing, the transfer of heat and material between the liquid and the catalyst surface is more rapid than in honeycomb structures consisting of straight, parallel canals. By means of the catalyst the linear velocities in the reactor may be lowered to below 3 m/S, since the static mixers disperse the hydrogen into the working solution even at low linear velocities, for example within the range 0.1-1.5 m/s. At these velocities the pressure loss and the mechanical wear of the catalyst coating are slight.
The catalyst activities in the static mixer according to the the present invention remain nearly unchanged for even long periods. This is in part due to a relatively open flow, in which case extensive impurities cannot adhere to the catalyst surface, the flow rinsing the canal walls clean. Likewise, the nearly anhydrous liquid phase and the oxygen-free gas phase promote the maintenance of the activity of the metal.
The length of the reactor is dependent on the mixer type used. When the canals of the static mixer are smaller, the geometric surface area of the mixer is greater, whereupon more catalyst layer per volume unit can be bound, but at the same tine the dynamic pressure loss in the mixer will be greater. Thus an optimum size can be found for the mixer canals.
By means of the invention, a high hydrogen peroxide yield is obtained as calculated in proportion to the active metal. This is due, first, to the fact that all of the catalyst is in that part of the reactor system in which the hydrogenation reaction takes place. In addition, the thin catalyst layer is advantageous for the exploiting of the active metal.
A more important advantage as compared to the closest comparable systems is the method of mixing the hydrogen and the working solution, which is advantageous in terms of the transfer of material and heat. Thus, uniform conditions are produced, which are advantageous for the selectivity and-speed of the hydrogenation reaction. By using a thin catalyst layer, the active metal can be used effectively in the hydrogenation and, furthermore, the contact period between the reagents and the catalyst remains short, factor which decreases the quantity of byproducts.
The hydrogenation process according to the invention can be implemented on an industrial scale so that the reduction is carried out in its entirety within an advantageous pressure range. The pressure in the reactor may be maintained within the range 1-15 bar, preferably 2-5 bar. The temperature of the working solution is maintained preferably below 1000C for example within the advantageous temperature range k 11 40-600c, for example in small-scale hydrogenation by jacket cooling of the reactor.
The invention may be carried into practice in various ways and some embodiments will now be described by way of illustration with reference to the accompanying drawings, in which the single figure depicts diagrammatically the hydrogenation process according to the invention, and the following example.
The hydrogenation step comprises a circulation tank 1, into which the working solution 14 to be hydrogenated is fed by means of a pump 4. The working solution is recycled to the circulation tank 1 by means of a pump 3 in the tube system 8 via a hydrogeiftatioii reactor 2 equipped with one or more static mixers 9 coated with a catalytic material. The hydrogenation reactor 2 is equipped with a cooling jacket 6, but it is clear that the cooling can be arranged in other ways as well. The working solution 14 to be hydrogenated can also be fed directly into the circulation tube system 8.
Hydrogen is introduced from a pipe 12 into the hydrogenation circulation tube system at a point somewhat before the hydrogenation reactor 2, and the exhaust gases are removed through a pipe 11, which is in the upper section of the circulation tank 1. Hydrogenated working solution is removed through a pipe 13 connected to the lower section of the circulation tank 1 and is fed via a pump 5 and an after-filter 7 to oxygenation. The hydrogenation conversion can be affected by adjusting the feeding rate of hydrogen 12, the pressure in the reactor, and the liquid flow 8 through it.
k 12 Exampl In the small-scale batch experiment which was carried out, a working solution was used which contained a 2-ethylanthraquinone 100 g/1. The solvent used was a mixture of aromatic hydrocarbons and an organic phosphorus compound. 10 static mixers coated with a catalytic material and having a length of 40 mm had been installed in the tubular reactor system, the length of which was approximately 400 mm and diameter 39 mm, in which case the reaction mixture was distributed effectively in relation to the cross sectional area of the tube, being mixed and at the same time catalyzed. A layer of about 50 micrometers of porous gamma-aluminium oxide carrier had been fixed to is the surface of the metallic static mixer. Palladium, in total approximately 0.5 percent by weight, had been absorbed into the aluminium oxide layer.
The flow rate of the working solution was approximately 2000 1/h, which corresponded to a linear velocity of 0.5 m/s. The temperature was 500C,,and the pressure at the beginning of the reactor was 4.0 bar.
Hydrogen was fed into the reactor at 55 1/h (NTP), only part of which was consumed in the reactor. The production of hydrogen peroxide in the reactor was on average 50 kg/(kg palladium) per hour.
Z7 13
Claims (14)
1. A process for the production of hydrogen peroxide by the anthraquinone process by circulating a reaction mixture into which there are fed hydrogen or a hydrogen- containing gas and a working solution, comprising an anthraquinone derivative in an organic solvent, via a static mixing zone, in order to hydrogenate the anthraquinone derivative in the presence of a solid catalyst, and by removing hydrogenated working solution and gas from the circulating reaction mixture, in which process the reaction mixture is mixed, while it is being catalyzed, by circulating the reacti-on mixture via a catalystcoated static mixing zone.
2. A process as claimed in claim 1, in which the static mixing zone is oblong.
3. A process as claimed in Claim 1 or Claim 2, in which the static mixing zone is continuous or made up of several parts.
4. A process as claimed in any preceding claim, in which in the static mixing zone, a pressure is maintained which is 1-15 bar.
5. A process as claimed in claim 4, in which the pressure maintained is 25 bar.
6. A process as claimed in any preceding claim, in which, in the static mixing zone, a temperature is maintained which is below 1000C.
7. A process as claimed in Claim 6, in which the t- 14 temperature maintained is 40-600C.
8. A process as claimed in any preceding claim, in which the reaction mixture is circulated through the static mixing zone at a velocity of 0.11.5 m/s.
9. A tubular static mixer, comprising one or several parts, for the catalytic hydrogenation of a reaction mixture which contains hydrogen or a hydrogen containing gas and a working solution comprising an anthraquinone derivative in an organic solvent, the static mixer being coated with a solid catalyst.
is
10. A static mixer as claimed in Claim 9, which is coated with a porous carrier into which a hydrogenation-catalyzing metal has been absorbed.
11. A static mixer as claimed in claim 10, in which the maximum thickness of the coating is approximately 300 um.
12. A static mixer as claimed in Claim 11, in which the minimum thickness of the coating is 5 um.
13. A static mixer as claimed in any of Claims 9 to 12., in which the porous carrier is active alumina, silica, silicate, and/or activated carbon.
14. A static mixer as claimed in any of Claims 9 to 13, in which hydrogenation-catalyzing palladium, platinum, rhodium and/or nickel has been absorbed into the mixer.
1 16. The use of a tubular static mixer, comprising one or several parts, for the catalytic hydrogenation of an anthraquinone derivative in an organic solvent by means of hydrogen or a hydrogen-containing gas, the surface of the static mixer having been coated with a porous carrier layer, preferably at maximum 300-umthick, into which a hydrogenationcatalyzing metal has been absorbed.
Published 1990 at TjiePatentoMce.8t4Lte House. 6671 High Holborn, London WC1R4TP. Further copies Maybe obtained from The Patent Office úsles Branch, St Mary Cray. Orp=4ton, Kent BR5 3RD. PrInted by Muluplex techwques JuL St MLry Cray, Kent. Con. 1187
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI890428A FI82669C (en) | 1989-01-27 | 1989-01-27 | FOERFARANDE FOER FRAMSTAELLNING AV VAETEPEROXID. |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB9001802D0 GB9001802D0 (en) | 1990-03-28 |
| GB2229173A true GB2229173A (en) | 1990-09-19 |
| GB2229173B GB2229173B (en) | 1993-03-03 |
Family
ID=8527797
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB9001802A Expired - Fee Related GB2229173B (en) | 1989-01-27 | 1990-01-26 | A process for the preparation of hydrogen peroxide |
Country Status (12)
| Country | Link |
|---|---|
| JP (1) | JPH02275703A (en) |
| AU (1) | AU620963B2 (en) |
| BR (1) | BR9000347A (en) |
| CA (1) | CA2008651A1 (en) |
| DE (1) | DE4002335A1 (en) |
| ES (1) | ES2019046A6 (en) |
| FI (1) | FI82669C (en) |
| FR (1) | FR2642412B1 (en) |
| GB (1) | GB2229173B (en) |
| IT (1) | IT1240869B (en) |
| NZ (1) | NZ232216A (en) |
| SE (1) | SE504578C2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001094006A3 (en) * | 2000-06-07 | 2003-10-30 | Abb Lummus Global Inc | Heat exchanger/reactor apparatus |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4313393C2 (en) * | 1993-04-07 | 2003-06-26 | Siemens Ag | Static mixer |
| FI95457C (en) * | 1994-03-15 | 1996-02-12 | Kemira Chemicals Oy | Process for the preparation of hydrogen peroxide and the reactor used therein |
| JP2022538553A (en) * | 2019-06-21 | 2022-09-05 | コモンウェルス サイエンティフィック アンド インダストリアル リサーチ オーガナイゼーション | Process for catalytically coating scaffolds |
| CN111410176A (en) * | 2020-05-14 | 2020-07-14 | 福建永荣科技有限公司 | Hydrogenation tower tubular reactor for producing hydrogen peroxide |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1227047A (en) * | 1968-05-16 | 1971-03-31 | ||
| US3615207A (en) * | 1969-06-16 | 1971-10-26 | Fmc Corp | Production of hydrogen peroxide by anthraquinone process |
| GB1312149A (en) * | 1969-07-12 | 1973-04-04 | Degussa | Process for the manufacturing of hydrogen peroxide |
| GB1348071A (en) * | 1970-08-27 | 1974-03-13 | Degussa | Hydrogen peroxide synthesis |
| GB1355394A (en) * | 1970-08-18 | 1974-06-05 | Mitsubishi Edogawa Kagaku Kk | Process for regenerating a degraded working solution for the production of hydrogen peroxide |
| GB1361665A (en) * | 1970-10-21 | 1974-07-30 | Fmc Corp | Processes for producing hydrogen peroxide |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL139013B (en) * | 1965-12-04 | 1973-06-15 | Degussa | PROCESS FOR PREPARING HYDROGEN PEROXIDE ACCORDING TO THE ANTRACHINO CIRCUIT PROCEDURE. |
| US4428922A (en) * | 1982-05-14 | 1984-01-31 | Fmc Corporation | Process for manufacturing hydrogen peroxide |
| SE431532B (en) * | 1982-09-08 | 1984-02-13 | Eka Ab | METHOD OF PRODUCING WHEAT PEROXIDE |
| FI77633B (en) * | 1986-12-05 | 1988-12-30 | Kemira Oy | FOERFARANDE FOER FRAMSTAELLNING AV VAETEPEROXID. |
-
1989
- 1989-01-27 FI FI890428A patent/FI82669C/en not_active IP Right Cessation
-
1990
- 1990-01-23 AU AU48660/90A patent/AU620963B2/en not_active Ceased
- 1990-01-23 SE SE9000227A patent/SE504578C2/en unknown
- 1990-01-24 NZ NZ232216A patent/NZ232216A/en unknown
- 1990-01-26 GB GB9001802A patent/GB2229173B/en not_active Expired - Fee Related
- 1990-01-26 DE DE4002335A patent/DE4002335A1/en not_active Withdrawn
- 1990-01-26 BR BR909000347A patent/BR9000347A/en not_active Application Discontinuation
- 1990-01-26 IT IT83314A patent/IT1240869B/en active IP Right Grant
- 1990-01-26 JP JP2015146A patent/JPH02275703A/en active Pending
- 1990-01-26 ES ES909000488A patent/ES2019046A6/en not_active Expired - Fee Related
- 1990-01-26 CA CA002008651A patent/CA2008651A1/en not_active Abandoned
- 1990-01-29 FR FR909000986A patent/FR2642412B1/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1227047A (en) * | 1968-05-16 | 1971-03-31 | ||
| US3615207A (en) * | 1969-06-16 | 1971-10-26 | Fmc Corp | Production of hydrogen peroxide by anthraquinone process |
| GB1312149A (en) * | 1969-07-12 | 1973-04-04 | Degussa | Process for the manufacturing of hydrogen peroxide |
| GB1355394A (en) * | 1970-08-18 | 1974-06-05 | Mitsubishi Edogawa Kagaku Kk | Process for regenerating a degraded working solution for the production of hydrogen peroxide |
| GB1348071A (en) * | 1970-08-27 | 1974-03-13 | Degussa | Hydrogen peroxide synthesis |
| GB1361665A (en) * | 1970-10-21 | 1974-07-30 | Fmc Corp | Processes for producing hydrogen peroxide |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001094006A3 (en) * | 2000-06-07 | 2003-10-30 | Abb Lummus Global Inc | Heat exchanger/reactor apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2642412A1 (en) | 1990-08-03 |
| FI890428A0 (en) | 1989-01-27 |
| FR2642412B1 (en) | 1992-11-13 |
| BR9000347A (en) | 1990-12-04 |
| ES2019046A6 (en) | 1991-05-16 |
| IT9083314A0 (en) | 1990-01-26 |
| FI82669C (en) | 1991-04-10 |
| NZ232216A (en) | 1991-10-25 |
| GB9001802D0 (en) | 1990-03-28 |
| AU4866090A (en) | 1990-08-02 |
| DE4002335A1 (en) | 1990-09-06 |
| FI890428A (en) | 1990-07-28 |
| IT1240869B (en) | 1993-12-17 |
| SE9000227L (en) | 1990-07-28 |
| CA2008651A1 (en) | 1990-07-27 |
| SE9000227D0 (en) | 1990-01-23 |
| SE504578C2 (en) | 1997-03-10 |
| GB2229173B (en) | 1993-03-03 |
| AU620963B2 (en) | 1992-02-27 |
| JPH02275703A (en) | 1990-11-09 |
| FI82669B (en) | 1990-12-31 |
| IT9083314A1 (en) | 1990-07-28 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19950126 |