EP1613574A1 - Verfahren zur herstellung von wenigstens einem partiellen oxidations- und/oder ammoxidationsprodukt eines kohlenwasserstoffs - Google Patents
Verfahren zur herstellung von wenigstens einem partiellen oxidations- und/oder ammoxidationsprodukt eines kohlenwasserstoffsInfo
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- EP1613574A1 EP1613574A1 EP04725618A EP04725618A EP1613574A1 EP 1613574 A1 EP1613574 A1 EP 1613574A1 EP 04725618 A EP04725618 A EP 04725618A EP 04725618 A EP04725618 A EP 04725618A EP 1613574 A1 EP1613574 A1 EP 1613574A1
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- Prior art keywords
- gas mixture
- hydrocarbon
- dehydrogenation
- heterogeneously catalyzed
- product gas
- Prior art date
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- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/63—Platinum group metals with rare earths or actinides
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
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- 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
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
- B01J23/622—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead
- B01J23/626—Platinum group metals with gallium, indium, thallium, germanium, tin or lead with germanium, tin or lead with tin
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C253/00—Preparation of carboxylic acid nitriles
- C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
- C07C253/26—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing carbon-to-carbon multiple bonds, e.g. unsaturated aldehydes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- 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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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- 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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a process for producing at least one partial oxidation and / or ammoxidation product of a hydrocarbon, in which at least one saturated hydrocarbon K is subjected to heterogeneously catalyzed dehydrogenation in the gas phase, a product gas mixture A being formed which contains at least one partially dehydrated hydrocarbon K.
- heterogeneously catalyzed dehydrogenation is understood to mean a dehydrogenation which is endothermic and in which hydrogen is formed as the primary by-product. It is carried out on solid catalysts which reduce the activation energy required for the thermal cleavage of a C-H bond.
- the heterogeneously catalyzed dehydrogenation differs from a heterogeneously catalyzed oxydehydrogenation in that the latter is forced by the presence of oxygen and water forms as a primary by-product.
- heterogeneously catalyzed oxide hydrogenation is exothermic.
- a complete oxidation of a hydrocarbon is to be understood to mean that the total carbon contained in this hydrocarbon is converted into oxides of carbon (CO, CO 2 ).
- Deviating reactions with oxygen are partial oxidations and partial ammoxidations in the presence of ammonia.
- the method described at the outset is known (cf., for example, DE-A 10219686, DE-A 10246119, DE-A 10245585, DE-A 10219685, EP-A 731077, DE-A 3313573, DE-A 10131297, DE-A 10211275, EP-A 117146, GB-A 2118939, US-A 4532365, US-A 3161670 and EP-A 193310) and is used, inter alia, for the production of acrolein, acrylic acid and / or acrylonitrile from propane, methacrolein, methacrylic acid and / or methacrylonitrile from iso -Butane applied.
- the partial ammoxidation differs from the partial oxidation essentially in the presence of ammonia in the onsgasgemisch.
- suitable selection of the ratio of NH 3 and 0 2 partial oxidation and partial ammoxidation can also be carried out side by side, ie, simultaneously.
- inert diluent gases By adding inert diluent gases, the reaction gas mixture of the partial oxidation and / or ammoxidation is kept outside the explosion area.
- the transition from product gas mixture A to product gas mixture A 'can take place by partially or completely removing any water vapor which may be present in product gas mixture A. This can e.g. by cooling the product gas mixture and partially or completely condensing out any water vapor it may contain.
- product gas mixture A can also be separated off to obtain a product gas mixture A '.
- the product gas mixture A can be passed over a membrane, which is generally designed as a tube, which is only permeable to hydrogen contained in the product gas mixture A and thus partially or completely separates the hydrogen contained in the product gas mixture A.
- CO 2 contained in product gas mixture A can be separated off by passing product gas mixture A through an aqueous alkali solution.
- An alternative separation method is absorption / desorption (stripping) according to DE-A 10245585.
- a disadvantage of the prior art methods is that neither the product gas mixture A, nor the product gas mixture A ⁇ nor the gas mixture B is subjected to the at least one heterogeneously catalyzed partial oxidation and / or ammoxidation in advance of a mechanical separation operation with which gas mixtures contained Solid particles can be separated from these gas mixtures. If an absorptive separation process is used, the absorbent may become saturated with solid particles over time. For example, when stripping and / or desorbing, the latter can then be carried along.
- catalysts suitable for heterogeneously catalyzed dehydrogenation normally also catalyze full combustion of hydrocarbons to CO 2 and H 2 O (see, for example, US Pat. No. 4,788,371) and the detonating gas reaction of H 2 with 0 2 to H 2 O. Both is disadvantageous in that it either leads to undesirable reactant consumption in the heterogeneously catalyzed partial oxidation and / or ammoxidation (which at the same time undesirably means additional heat build-up) or involves risks that are difficult to assess.
- the object of the present invention was therefore to provide a more advantageous procedure which is also particularly suitable for safe, continuous operation over comparatively long periods of time (the service life of catalysts for heterogeneously catalyzed partial oxidations and / or ammoxidations is usually a few years).
- a process for the production of at least one partial oxidation and / or ammoxidation product of a hydrocarbon in which at least one saturated hydrocarbon K is subjected to heterogeneously catalyzed dehydrogenation in the gas phase, producing a product gas mixture A which comprises at least one partially dehydrogenated hydrocarbon K, components contained in the product gas mixture A, different from the saturated hydrocarbon K and from the partially dehydrated hydrocarbon K, are left therein or partially or completely separated off to obtain a product gas mixture A ', and product gas mixture A and / or product gas mixture A' as part of a gas mixture B at least one heterogeneously catalyzed partial oxidation and / or ammoxidation of the at least one partially dehydrated hydrocarbon K contained in the product gas mixture A and / or product gas mixture A ', was found, which is characterized in that d the product gas mixture A, the product gas mixture A 5 and / or the gas mixture B are subjected to the at least one heterogeneously catalyze
- the process according to the invention is particularly advantageous if product gas mixture A as such and / or product gas mixture A 'is also used in the process of heterogeneously catalyzed partial oxidation and / or ammoxidation, which is obtained from product gas mixture A in that, as a rule, in the same contained or partially condensed water vapor.
- Gas purifiers suitable according to the invention using a mechanical separation operation are e.g. Chamber, impact and centrifugal separators that use mass forces.
- acoustic separators can also be used for the method according to the invention. Aerocyclones are preferred.
- filtering can also be carried out in a simple manner as a mechanical separation operation. Filter fabrics, porous filter materials, paper fleece or oil-wetted metal filters can be considered as filter layers. Electrical separators can also be used according to the invention.
- the gas mixture can also flow through an inert fixed bed by separating the finest solid particles contained in the gas mixture before the gas mixture reaches the catalyst for the heterogeneously catalyzed partial oxidation and / or ammoxidation.
- mechanical separation operation is also intended to include spray devices in which the gas is exposed to liquid droplets in cocurrent or countercurrent (e.g. from high-boiling organic liquids or from water) which are able to absorb solid particles contained in the gas. The spray liquid is exchanged after a few recirculations to avoid saturation with solid particles.
- the heterogeneously catalyzed dehydrogenation of the saturated hydrocarbon K according to the invention (in particular in the case of propane and / or isobutane) as described in DE-A 3313973, WO 01/96270, DE-A 10131297 or DE-A 10211275 be performed.
- the conversion can be increased by lowering the partial pressure of the products.
- This can be achieved in a simple manner, for example by dehydrogenation under reduced pressure and / or by admixing essentially inert diluent gases, such as water vapor, which is normally an inert gas for the dehydrogenation reaction.
- Dilution with water vapor is another advantage in usually a reduced coking of the catalyst used, since the water vapor reacts with coke formed according to the principle of coal gasification.
- water vapor can be used as the dilution gas in the subsequent at least one oxidation and / or ammoxidation zone.
- water vapor can also be partially or completely separated from the product mixture A of the dehydrogenation in a simple manner (for example by condensation), which opens up the possibility of further using the product mixture A ′ available in the at least one partial oxidation and / or amoxidation To increase the proportion of the diluent gas N 2 .
- diluents suitable for heterogeneously catalyzed dehydrogenation are, for example, CO, methane, ethane, CO 2 , nitrogen and noble gases such as He, Ne and Ar. All of the diluents mentioned can be used either individually or in the form of a wide variety of mixtures.
- the diluents mentioned are generally also suitable diluents in the at least one partial oxidation and / or amoxidation.
- Inert diluents are, in particular, inert diluents (ie less than 5 mol%, preferably less than 3 mol% and even better less than 1 mol%) of chemically changing diluents.
- all dehydrogenation catalysts known in the prior art are suitable for heterogeneously catalyzed dehydrogenation. They can be roughly divided into two groups. Namely in those which are oxidic in nature (for example chromium oxide and / or aluminum oxide) and in those which are composed of at least one, generally comparatively noble, metal (for example platinum, palladium, Tin, gold, silver).
- dehydrogenation catalysts can be used which are described in WO 01/96270, EP-A 731077, DE-A 10211275, DE-A 10131297, WO 99/46039, US-A 4788 371, EP-A -0 705 136, WO 99/29420, US-A 4 220 091, US-A 5430 220, US-A 5 877 369, EP-A-0 117 146, DE-A 199 37 196 , DE-A 199 37 105 and DE-A 199 37 107 are recommended.
- both the catalyst according to Example 1, Example 2, Example 3 and Example 4 of DE-A 199 37 107 can be used.
- dehydrogenation catalysts which contain 10 to 99.9% by weight of zirconium dioxide, 0 to 60% by weight of aluminum oxide, silicon dioxide and / or titanium dioxide and 0.1 to 10% by weight of at least one element of the first or second Main group, an element of the third subgroup, an element of the eighth subgroup of the Periodic Table of the Elements, containing lanthanum and / or tin, with the proviso that the sum of the weight percent is 100% by weight.
- all reactor types and process variants known in the prior art can be used to carry out the heterogeneously catalyzed dehydrogenation according to the invention. Descriptions of such process variants include, for example, all the prior art documents cited with regard to the dehydrogenation catalysts.
- dehydrogenation processes suitable according to the invention also contains "Catalytica® Studies Division, Oxidative Dehydrogenation and Alternative Dehydrogenation Processes, Study Number 4192 OD, 1993, 430 Ferguson Drive, Mountain View, California, 94043-5272 U.S.A ..
- reaction gas mixture which contains the saturated hydrocarbon K to be dehydrogenated and which is to be dehydrogenated can be diluted with water vapor for heterogeneously catalyzed dehydrogenation at elevated temperature.
- Deposited carbon is partially or completely eliminated under the given conditions according to the principle of coal gasification.
- Another way of eliminating deposited carbon compounds is to flow through the dehydrogenation catalyst from time to time at elevated temperature with an oxygen-containing gas and thus virtually burn off the deposited carbon.
- an oxygen-containing gas e.g. propane or isobutane
- it is also possible to largely suppress the formation of carbon deposits by adding molecular hydrogen to the saturated hydrocarbon K (e.g. propane or isobutane) to be dehydrogenated under heterogeneous catalysis before it is passed over the dehydrogenation catalyst at elevated temperature.
- K saturated hydrocarbon K
- a suitable reactor form for the heterogeneously catalyzed dehydrogenation according to the invention is the fixed bed tube or tube bundle reactor.
- the dehydrogenation catalyst is located in one or in a bundle of reaction tubes as a fixed bed.
- the reaction tubes are heated in that a gas, for example a hydrocarbon such as methane, is burned in the space surrounding the reaction tubes. It is favorable to apply this direct form of contact tube heating only to the first approximately 20 to 30% of the fixed bed filling and to heat the remaining bed length to the required reaction temperature by means of the radiant heat released during the combustion. In this way, an almost isothermal reaction can be achieved.
- Suitable inner tube diameters are about 10 to 15 cm.
- a typical tube bundle dehydrogenation reactor comprises 300 to 1000 reaction tubes.
- the temperature in the interior of the reaction tube is in the range from 300 to 700 ° C., preferably in the range from 400 to 700 ° C.
- the reaction gas starting mixture is advantageously fed to the tubular reactor preheated to the reaction temperature. It is possible that the product gas mixture leaves the reaction tube at a temperature which is 50 to 100 ° C lower. However, this initial temperature can also be higher or at the same level.
- the use of oxidic dehydrogenation catalysts based on chromium and / or aluminum oxide is expedient. Often you will not use a diluent gas, but will start with saturated hydrocarbon K (e.g. propane or crude propane) as the starting reaction gas.
- saturated hydrocarbon K e.g. propane or crude propane
- Such a procedure can also be used in the so-called “steam active reforming (STAR) process", which was developed by Phillips Petroleum Co. (cf. Example US-A 4 902 849, US-A 4 996 387 and US-A 5 389 342).
- Platinum on zinc (magnesium) spinel containing promoters is advantageously used as the dehydrogenation catalyst in the STAR process (see, for example, US Pat. No. 5,073,662).
- propane to be dehydrogenated is diluted with water vapor in the STAR process.
- a molar ratio of water vapor to propane in the range from 4 to 6 is typical.
- the reactor outlet pressure is frequently 3 to 8 atm and the reaction temperature is expediently chosen to be 480 to 620 ° C.
- Typical catalyst loads with the total reaction gas mixture are 0.5 to 10 h "1 (LHSV).
- the heterogeneously catalyzed dehydrogenation according to the invention can also be designed in a moving bed.
- the moving catalyst bed can be accommodated in a radial flow reactor.
- the catalyst slowly moves from top to bottom while the reaction gas mixture flows radially. This procedure is used, for example, in the so-called UOP-Oleflex dehydrogenation process. Since the reactors are operated practically adiabatically in this process, it is expedient to operate several reactors connected in series as a cascade (typically up to four).
- reaction gas inlet mixture acts as a heat carrier, on the heat content of which the drop in the reaction temperature depends) and still achieve attractive overall conversions.
- a spherical dehydrogenation catalyst which essentially consists of platinum on a spherical alumina support can be used as the dehydrogenation catalyst for this process.
- hydrogen is added to the saturated hydrocarbon K (eg propane) to be dehydrogenated in order to avoid premature catalyst aging.
- the working pressure is typically 2 to 5 atm.
- propane the hydrogen to propane ratio (molar) is suitably 0.1 are to 1.
- the reaction temperatures preferably from 550 to 650 ° C and the contact time of the catalyst with reaction gas mixture is chosen to be about 2 to 6 h '1.
- the catalyst geometry can also be spherical, but also cylindrical (hollow or solid) or otherwise geometrically designed.
- two fluidized beds are operated side by side, one of which can be in the state of regeneration at times without having any negative effects on the overall process.
- Chromium oxide on aluminum oxide is used as the active material.
- the working pressure is typically 1 to 2 atm and the dehydration temperature is usually 550 to 600 ° C.
- the heat required for the dehydrogenation is introduced into the reaction system by preheating the dehydrogenation catalyst to the reaction temperature.
- the above dehydration method is also known in the literature as the Snamprogetti-Yarsintez method.
- heterogeneously catalyzed dehydrogenation with extensive exclusion of oxygen can also be carried out by a process developed by ABB Lummus Crest (see Proceedings De Witt, Petrochem. Review, Houston, Texas, 1992, P1).
- a common feature of the heterogeneously catalyzed dehydrogenation processes of a saturated hydrocarbon K with extensive exclusion of oxygen described so far is that they are operated with saturated hydrocarbon K (for example propane) conversions of> 30 mol% (generally ⁇ 60 mol%) (based on single reaction zone passage). It is advantageous according to the invention that it is sufficient to achieve a saturated hydrocarbon K (e.g. propane) conversion of 5 5 mol% to 30 30 mol% or 25 25 mol%. This means that the heterogeneously catalyzed dehydrogenation can also be operated at conversions of 10 to 20 mol% (the conversions relate to a single reaction zone passage).
- the molar ratio of molecular hydrogen to saturated hydrocarbon K is generally ⁇ 5.
- the molar ratio of water vapor to saturated hydrocarbon K can accordingly be ⁇ 0 to 30, expediently 0.1, with a comparatively low hydrocarbon K conversion to 2 and cheap 0.5 to 1. It has also proven to be advantageous for a procedure with a low dehydrogenation conversion that only a comparatively low amount of heat is consumed when the reaction gas is passed through once and that comparatively low reaction temperatures are sufficient to achieve the conversion with a single passage of the reactor.
- reaction gas starting mixture will generally first be heated to a temperature of 500 to 700 ° C (or 550 to 650 ° C) (for example by direct firing of the surrounding wall). Normally, a single adiabatic passage through a catalyst bed will then be sufficient to achieve the desired conversion, the reaction gas mixture cooling down by about 30 ° C. to 200 ° C. (depending on conversion and dilution).
- the presence of water vapor as a heat transfer medium also has an advantageous effect from the point of view of an adiabatic driving style. The lower reaction temperature enables longer service life of the catalyst bed used.
- the heterogeneously catalyzed dehydrogenation with comparatively low conversion can be carried out both in a fixed bed reactor and in a moving bed or fluidized bed reactor.
- a single shaft furnace reactor is sufficient as a fixed bed reactor, through which the reaction gas mixture flows axially and / or radially.
- this is a single closed reaction volume, for example a container, the inside diameter of which is 0.1 to 10 m, possibly also 0.5 to 5 m, and in which the fixed catalyst bed is mounted on a carrier device (for example a grating) is applied.
- the reaction volume charged with catalyst which is thermally insulated in adiabatic operation, is flowed through axially by the hot reaction gas containing saturated hydrocarbon K.
- the catalyst geometry can be spherical, ring-shaped or strand-shaped. In this case, since the reaction volume can be achieved using a very inexpensive apparatus, all catalyst geometries which have a particularly low pressure drop are preferred.
- the reactor can consist, for example, of two cylindrical grids located concentrically one inside the other in a jacket shell and the catalyst bed can be arranged in the annular gap thereof.
- the metal shell would in turn be thermally insulated.
- Suitable catalysts for a heterogeneously catalyzed dehydrogenation with comparatively low conversion in a single pass are, in particular, the catalysts disclosed in DE-A 19937 107, especially all of the examples disclosed.
- the aforementioned catalysts can be regenerated in a simple manner, for example, by first diluting air with nitrogen and / or water vapor (preferably) at an inlet temperature of 300 to 600 ° C, often at 400 to 550 ° C the catalyst bed conducts.
- the catalyst load with regeneration gas can be, for example, 50 to 10,000 h -1 and the oxygen content of the regeneration gas can be 0.5 to 20% by volume.
- air can be used as the regeneration gas under otherwise identical regeneration conditions.
- inert gas for example N 2
- the heterogeneously catalyzed dehydrogenation with comparatively low conversion can be operated in all cases with the same catalyst loads (both for the reaction gas as a whole and for the saturated hydrocarbon K contained in it) as the variants with high conversion (> 30 mol%).
- This exposure to reaction gas can be, for example, 100 to 10,000 h " , often 300 to 5000 h " 1 , that is to say in many cases approximately 500 to 3000 h "1 .
- the heterogeneously catalyzed dehydrogenation can be carried out in a particularly elegant manner with comparatively low conversion in a tray reactor.
- This spatially contains more than one catalyst bed catalyzing the dehydrogenation.
- the number of calibrator beds can be 1 to 20, suitably 2 to 8, but also 3 to 6.
- the Kalalyzer beds are preferably arranged radially or axially one behind the other. Appropriately in terms of use, the fixed catalyst bed type is used in such a tray reactor.
- the fixed catalyst beds are arranged axially in a shaft furnace reactor or in the annular gaps of centrally arranged cylindrical gratings.
- the reaction gas mixture is expediently subjected to intermediate heating in the tray reactor on its way from one catalyst bed to the next catalyst bed, for example by transferring heat exchanger fins heated with hot gases or by passing through tubes heated with hot fuel gases.
- the tray reactor is operated adiabatically, it is sufficient for the desired conversions (30 30 mol%), especially when using the catalysts described in DE-A 19937 107, in particular the exemplary embodiments, to a temperature of Pre-heated 450 to 550 ° C in the dehydrogenation reactor and keep within the tray reactor in this temperature range. This means that the entire dehydrogenation can be carried out at extremely low temperatures, which has proven particularly favorable for the service life of the fixed catalyst beds between two regenerations.
- the heat of reaction released in this way enables, in a quasi-autothermal manner, an almost isothermal mode of operation of the heterogeneously catalyzed dehydrogenation.
- dehydrogenation with decreasing or essentially constant temperature is possible, which enables particularly long standing times between two regenerations.
- an oxygen feed as described above should be carried out in such a way that the oxygen content of the reaction gas mixture, based on the amount of saturated hydrocarbon K contained therein, is 0.5 to 30% by volume.
- the resulting combustion gases generally have an additional dilution effect and thereby promote heterogeneously catalyzed dehydration.
- the isothermal nature of the heterogeneously catalyzed dehydrogenation can be further improved by installing in the tray reactor in the spaces between the catalyst beds, which, before being filled, are advantageously but not necessarily evacuated internals (for example tubular). Such internals can also be placed in the respective catalyst bed. These internals contain suitable solids or liquids that evaporate or melt above a certain temperature, consuming heat and condensing again where the temperature falls below, thereby releasing heat.
- One way of heating the reaction gas starting mixture for the heterogeneously catalyzed dehydrogenation to the required reaction temperature is also to burn part of the saturated hydrocarbon K and / or H 2 contained therein by means of molecular oxygen (for example on suitable specific-action combustion catalysts, for example, by simply passing over and / or passing through) and by means of the heat of combustion thus released to bring about the heating to the desired reaction temperature.
- the resulting combustion products such as CO 2 , H 2 O and the N 2 which may accompany the molecular oxygen required for the combustion, advantageously form inert diluent gases.
- the aforementioned hydrogen combustion can be implemented particularly elegantly, as described in DE-A 10211275. That is, in a process of continuous heterogeneously catalyzed partial dehydrogenation of saturated hydrocarbon K in the gas phase, in which
- reaction gas containing the reaction gas to be dehydrogenated saturated hydrocarbon K is fed continuously
- the reaction gas is passed in the reaction zone over at least one fixed catalyst bed on which molecular hydrogen and at least partially dehydrogenated hydrocarbon K are formed by catalytic dehydrogenation,
- At least one gas containing molecular oxygen is added to the reaction gas before and / or after entering the reaction zone,
- the molecular oxygen in the reaction gas contained in the reaction gas partially oxidizes to water vapor and
- a product gas is removed from the reaction zone, the molecular hydrogen, water vapor, partially dehydrated hydrocarbon K and saturated
- product gas mixture A which is characterized in that the product gas withdrawn from the reaction zone is divided into two portions of identical composition and one of the two portions is recycled as circulating gas into the dehydrogenation reaction zone and the other portion is used according to the invention as product gas mixture A.
- Variants of the catalytic dehydrogenation to be used according to the invention described above can be used in particular if the saturated hydrocarbon K to be dehydrogenated is propane and / or isobutane.
- the product gas mixture A and / or the product gas mixture A 'to be produced from the same as described can now be used in a manner known per se for charging a heterogeneously catalyzed partial oxidation and / or ammoxidation with a gas mixture B (cf. prior art cited at the beginning). It is only essential to the invention that the product gas mixture A, the product gas mixture A 'and / or the mixture B are subjected to a mechanical separation operation beforehand with the at least one heterogeneously catalyzed partial oxidation and / or ammoxidation the solid particles contained in these gas mixtures can be separated from these gas mixtures.
- Partial oxidation for the process according to the invention is in particular the partial oxidation of propene (obtained by partial dehydrogenation of propane) to acrolein and / or acrylic acid and the partial oxidation of isobutene (obtained by partial dehydrogenation of isobutane) to methacrolein and / or methacrylic acid.
- the partial ammoxidation for the process according to the invention is in particular the partial ammoxidation of propene to acrylonitrile and the partial ammoxidation of isobutene to methacrylonitrile.
- Zr0 2 • SiO 2 mixed oxide carrier (strands with a length in the range from 3 to 8 mm and a diameter of 2 mm; produced in accordance with Example 3 of DE-A 10219879) was applied in a manner similar to that in FIG DE-
- a 10219879 described a Pt Sn alloy applied, which had a doctorate with the elements Cs, K and La in oxidic form.
- the element stoichiometry (mass ratio) was: Pto , 3 Sn 0 , 6 la 3> oCso, 5 Ko, 2 (Zr ⁇ 2 ) 88> 3 (Si0 2 ) 7Fl .
- the alloy with the doctorate as described was applied by soaking the split support with salt solutions of the corresponding metals and subsequent thermal treatment (1.5 h) at 560 ° C. in an air stream.
- thermal treatment 1.5 h
- both the active components Pt and Sn and the promoters were converted into their oxidic form.
- the active components of the catalyst precursor were reduced to the metals as described below in a hydrogen stream at 500 ° C. to obtain the active catalyst.
- the bottom of the reaction tube was covered over a length of 1000 mm on its outer wall with a microporous insulating material of the type MPS-Super G from Mientherm, DE and the layer thickness 100 mm (quasi-adiabatic reaction part).
- the heating functioned only as a backup heater, while in the upper area it was used for direct heating of the pipe section.
- the catalyst precursor was activated in a hydrogen stream as described in Example 1 of DE-A 10211275.
- the test facility consisted of 4 parts:
- Discharge unit In the metering unit, the liquid starting materials LPG and water (if necessary in a nitrogen stream) were passed through an evaporator W100 and converted into the gas phase in the same. After the evaporator, if necessary, air, molecular oxygen and molecular hydrogen could be mixed into the gas mixture generated in the evaporator while maintaining the desired fresh starting mixture.
- the fresh starting mixture (possibly in a mixture with circulating gas) was heated in a preheater (heat exchanger) W200 to a temperature of 400 to 500 ° C. and then passed into the described dehydrogenation reactor C330 (from top to bottom).
- the heating zones had the following temperatures from top to bottom: 500 ° C, 550 ° C, 550 ° C and 550 ° C.
- the inlet pressure into the dehydrogenation reactor was chosen to be 2 bar.
- the product gas mixture A leaving the dehydrogenation reactor was passed through an air-cooled heat exchanger and cooled to 300.degree. It was then passed wholly or partially into the discharge section via a guide tube and processed further in the same. If only part of the cooled product gas mixture A was fed into the discharge section, the remaining part was fed to the cycle gas unit.
- the circulated part of the product gas mixture A was first further cooled to 150 ° C. in a heat exchanger W420 operated with heat transfer oil, subsequently recompressed to 2 bar in a compressor V440 and then after passing through a heat exchanger W460, where it heated to 300 ° C. was combined with fresh starting gas mixture upstream of the W200 preheater (and then fed to the preheater).
- the test facility was operated essentially continuously over a period of 3 months. A total of 26 reaction cycles were carried out. After each reaction cycle, the dehydrogenation catalyst was regenerated in accordance with DE-A 10028582 with the sequence rinsing, burning off, rinsing, reducing. The conditions were kept constant within a reaction cycle (the shortest duration of a reaction cycle was 3 h and the longest duration of a reaction cycle was 100 h). The conditions of all cycles were in the following grid:
- Cycle duration 3 - 100 h; LPG amount: 500 - 2000 g / h; Fresh water vapor: 500 - 1000 g / h;
- Circular gas ratio 0 or 5 (ratio of the quantity circulated to the quantity omitted)
- the parts of the test facility that were exposed to temperatures of up to 300 ° C were made of V2A steel.
- the parts of the test facility that were exposed to temperatures above 300 ° C were made of 1.4841 steel.
- the analysis of the rust film using atomic absorption spectroscopy showed the expected components Fe, Ni and Cr as well as Zr, Si and Pt that could only come from the dehydrogenation catalyst. Overall, the analyzed rust sample showed the following element amounts:
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Abstract
Description
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Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
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DE10316039A DE10316039A1 (de) | 2003-04-07 | 2003-04-07 | Verfahren zur Herstellung von wenigstens einem partiellen Oxidations-und/oder Ammoxidationsprodukt eines Kohlenwasserstoffs |
US47616603P | 2003-06-06 | 2003-06-06 | |
PCT/EP2004/003557 WO2004089858A1 (de) | 2003-04-07 | 2004-04-03 | Verfahren zur herstellung von wenigstens einem partiellen oxidations- und/oder ammoxidationsprodukt eines kohlenwasserstoffs |
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EP1613574A1 true EP1613574A1 (de) | 2006-01-11 |
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EP04725618A Withdrawn EP1613574A1 (de) | 2003-04-07 | 2004-04-03 | Verfahren zur herstellung von wenigstens einem partiellen oxidations- und/oder ammoxidationsprodukt eines kohlenwasserstoffs |
Country Status (7)
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EP (1) | EP1613574A1 (de) |
JP (1) | JP2006522063A (de) |
KR (1) | KR20050122239A (de) |
BR (1) | BRPI0408968A (de) |
MY (1) | MY144309A (de) |
RU (1) | RU2356881C2 (de) |
WO (1) | WO2004089858A1 (de) |
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US7388106B2 (en) * | 2005-10-14 | 2008-06-17 | Basf Aktiengesellschaft | Process for preparing acrolein or acrylic acid or a mixture thereof from propane |
DE102005052923A1 (de) * | 2005-11-03 | 2007-05-10 | Basf Ag | Verfahren zum stabilen Betreiben eines kontinuierlich ausgeübten Herstellprozesses zur Erzeugung von Acrolein, oder Acrylsäure oder deren Gemisch aus Propan |
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US3161670A (en) * | 1960-12-12 | 1964-12-15 | Shell Oil Co | Preparation of olefinic compounds |
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2004
- 2004-04-03 JP JP2006504983A patent/JP2006522063A/ja not_active Withdrawn
- 2004-04-03 WO PCT/EP2004/003557 patent/WO2004089858A1/de active Application Filing
- 2004-04-03 BR BRPI0408968-5A patent/BRPI0408968A/pt not_active IP Right Cessation
- 2004-04-03 RU RU2005134010/04A patent/RU2356881C2/ru not_active IP Right Cessation
- 2004-04-03 KR KR1020057018981A patent/KR20050122239A/ko not_active Application Discontinuation
- 2004-04-03 EP EP04725618A patent/EP1613574A1/de not_active Withdrawn
- 2004-04-05 MY MYPI20041246A patent/MY144309A/en unknown
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See references of WO2004089858A1 * |
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RU2005134010A (ru) | 2006-05-27 |
WO2004089858A1 (de) | 2004-10-21 |
BRPI0408968A (pt) | 2006-04-04 |
MY144309A (en) | 2011-08-29 |
JP2006522063A (ja) | 2006-09-28 |
RU2356881C2 (ru) | 2009-05-27 |
KR20050122239A (ko) | 2005-12-28 |
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