JP2008531261A - Manufacturing process, manufacturing system, and catalyst composition - Google Patents

Abstract

The disclosed embodiments provide a catalyst composition that can have a substrate, chromium, and at least one alkali metal. A manufacturing process is provided for removing a catalyst composition from a solution comprising a catalyst composition having an alkali metal composition and a substrate. Also provided is a manufacturing process that can have contacting a compound with a reagent in the presence of a catalyst composition. A manufacturing system is also provided that has a reactor connected to both a reactant vessel and a reagent vessel, the reactor having a catalyst composition comprising chromium and at least one alkali metal.

Description

(Claiming priority)
This application claims priority for US Provisional Application No. 60 / 656,600, entitled “Halogenation Process”, filing date February 25, 2005, which is incorporated herein by reference.

(Technical field)
This disclosure relates to halogenation steps, systems, and manufacturing processes, systems, and catalyst compositions having a halogenated catalyst composition.

(Background of the Invention)
A chemical manufacturing process can include the use of a catalyst composition to improve the manufacturing process. The catalyst composition not only facilitates the reaction of the reactants themselves, but in some instances can improve the reaction efficiency of the reactants, for example, to provide a more pure product more efficiently. The halogenation step including halogenation substitution and a combination of halogenation substitution and elimination reaction is a reaction that can utilize the catalyst composition. The catalyst composition helps to make these halogenation steps more efficient, for example by allowing halogen substitution, from chlorine compounds to fluorine compounds, bromine compounds to chlorine compounds, iodine compounds to bromine compounds, iodine compounds to fluorine. Even fluorine compounds can be produced from compounds and bromine compounds.

  A typical catalytic reaction can occur at a temperature at which the reactants are in the gas phase. These catalytic gas phase reactions can degrade the catalyst composition and require frequent reactivation and replacement of the composition to meet reaction efficiency requirements, and are produced during catalyst activation and replacement. The process needs to be stopped. During the manufacturing process, catalyst compositions that can facilitate efficient reaction of the reactants without frequent reactivation or exchange are useful.

(Overview)
The disclosed examples provide a catalyst composition that can have a base, chromium, and at least one alkali metal. The manufacturing process can include making a first solution having an alkali metal composition and contacting the first solution with a base to form a second solution having the base and the alkali metal composition. This step can further comprise removing the catalyst composition having the alkali metal composition and the base from the second solution.

  Also provided is a manufacturing process that can include contacting a compound with a reagent in the presence of a catalyst composition having a base, chromium, and at least one alkali metal.

  According to an exemplary embodiment, the C-3 compound can be contacted with a reagent in the presence of a catalyst composition having at least one alkali metal.

  A manufacturing system is also provided that has a reactor connected to both a reactant vessel and a reagent vessel, the reactor having a catalyst composition comprising chromium and at least one alkali metal.

(Description of Examples)
The catalyst composition, manufacturing process and system will be described with reference to the drawings. Referring to the figure, a manufacturing system 10 is shown having a reactor 12 connected to both a reactant container 14 and a reagent container 16. Reactor 12 is further connected to product vessel 18, and in an exemplary embodiment, reactor 12 has a catalyst composition 20. The system 10 can be configured as an industrial chemical manufacturing system. For example, the flow of reactants from the reactant container 14 and the reagent from the reagent container 16 can be controlled using a flow meter, and these reactants can also be passed through a vaporizer where the system 10 is vaporized. Configure the reagent to contact the reactants in phase. The reactor 12 is sometimes referred to as a reaction chamber, and the reaction chamber includes an interior that regulates the volume of the chamber. The reactor 12 of the system 10 can also be configured to maintain the temperature of the contents of the reactor 12. Such a temperature can be maintained, for example, by coating the reactor 12 with a steam heat jacket. The product flowing from the reactor 12 to the product container 18 can be controlled, for example, by gas cooling of the reactor 12 in the condenser.

  As shown in a typical figure, the system 10 is constructed using vessels 14 and 16 connected to the reactor 12 from the lower portion of the reactor 12 and the product is removed from the upper portion of the reactor 12. This should not be considered the only configuration of system 10. The system 10 is configured to flow reactants and reagents downward from the upper portion of the reactor 12, and the product can also be removed from the lower portion of the reactor 12. The reactant in the reactant container 14 and the reagent in the reagent container 16 can also be supplied or provided to the reactor 12 by the pressure difference between the one in the reactor 12 and the one in the containers 14 and 16. According to an exemplary embodiment, vessels 14 and 16 can be maintained at a higher pressure, for example, by a backing gas such as nitrogen, which can provide a higher pressure to reactor 12 maintained at a lower pressure. The flow of reactant is caused by the pressure difference supplied. For example, in certain embodiments, reactor 12 is maintained at a pressure of 687 kPa.

According to another embodiment, the system 10 can have an oxidant vessel 22 connected to the reactor 12. The oxidizing agent in the oxidizing agent container 22 is supplied at a predetermined supply rate together with the reactant in the reactant container 14 and the reagent in the reagent container 16. The oxidant container 22 can be connected directly to the reactor 12 or can be connected to a conduit connecting the reactant container 14 and the reagent container 16 to the reactor 12. In an exemplary embodiment, all reactants and vessel conduits connected to the reactor 12 can also be connected to each other before connecting to the reactor 12. The oxidizing agent can have O or Cl in the form of O ₂ or Cl ₂ . The oxidant is supplied to the reactor 12 as a molar fraction of reactant and reagent. For example, the molar fraction of oxidant may be at least about 0.1% of the combined total of oxidant, reagents, and reactants provided to reactor 12. As another example, the molar fraction of oxidant may be about 0.1-0.3%. The oxidant can be provided during activation or preparation of the catalyst composition 20 or after activation of the catalyst composition 20 with the reactants.

  As shown in the typical figure, the catalyst composition 20 is contained within the reactor 12. In the illustrated embodiment, the catalyst composition 20 is present within the volume of the reactor 12. However, the catalyst composition 20 can be present, for example, with the walls of the reactor 12 or in the middle thereof. In an exemplary embodiment, reactor 12 is constructed from stainless steel and can take a tubular shape, such as a pipe. In other exemplary implementations, the reactor 12 can also be composed of inconel®, monel® carbon steel or nickel. A mesh net (not shown) may be provided in the lower part of the reactor 12. The composition 20 can also be provided, for example, in the reactor 12 on this mesh network.

  The catalyst composition 20 can have chromium and at least one alkali metal. The catalyst composition 20 can also have a base. The base can have the inner wall of the reactor 12 and carbon or other substrates known to those skilled in the art. According to an exemplary embodiment, the substrate can have activated carbon. In a specific example, for example, the substrate of the catalyst composition 20 is Takeda brand activated carbon (Takeda Pharmaceutical Co., Ltd., Japan 103-8868, Nihonbashi 2-chome 12-10-10, Chuo-ku, Tokyo) or Calgon brand carbon (Calbon Carbon Corporation). , 400 Calgon Carbon Drive Pittsburgh, PA. 15205). The alkali metal can have, for example, potassium and other alkali metals of Group I of the Periodic Table of Elements. In an exemplary embodiment, the molar ratio of chromium to one alkali metal in the catalyst composition may be at least about 50: 1.

  The catalyst composition 20 can be manufactured by making a first solution having an acid composition. According to an exemplary embodiment, the acid composition can be chromic acid and can provide the majority of the chromium in the catalyst composition. The first solution can have a solvent such as water.

  The second solution having the alkali metal composition is made separately and then combined with the first solution or the first solution of the acid composition, for example, to constitute the second solution. According to a typical implementation, the second solution can have a solvent such as water. It is envisioned that other solvents may be similarly utilized for the first and second solutions. The alkali metal composition can have potassium and chromium or oxygen. The alkali metal composition may be an alkali metal salt comprising an alkali metal salt of chromic acid such as potassium dichromate, ie K2Cr2O7. Alkali metal salts of other acids may be included in the alkali metal composition. The alkali metal composition of the alkali metal solution may be, for example, at least 4% (weight ratio).

  In preparing the first and second solutions, the solutions can be combined as necessary to form a third solution having a solvent, an acid composition, and an alkali metal composition. The third solution is also called a chromium-alkali metal solution. These solutions are made by stirring the solvent and the composition to form a solution of the composition according to a typical implementation. Containers suitable for such mixing include plastic and glass containers, for example, mixing is achieved using a magnetic stir bar.

The chromium-alkali metal solution can be combined with the substrate to constitute a catalyst solution. As described above, the substrate can have carbon such as Takeda or Calgon carbon or activated carbon. According to a typical implementation, the substrate is provided to the tumbler apparatus in a substantially dry form. The chromium-alkali metal solution is combined with the substrate in the apparatus and mixed using the apparatus to form a catalyst solution. The catalyst solution can have, for example, CrO ₃ / K ₂ CrO ₇ / activated carbon in a weight ratio of about 10.8 / 0.6 / 30/23. According to an exemplary embodiment, combining the substrate and the chromium-alkali solution can result in an exotherm. The resulting exotherm may be sufficient to separate a sufficient amount of solvent from the catalyst solution. According to a typical implementation, mixing the catalyst solution and the exotherm can separate most of the solvent from the catalyst solution, while other implementations remove all but a trace amount of solvent and have a catalyst composition with ppm amounts of solvent. Leave.

  In an exemplary embodiment, the amount of alkali metal composition used to produce the catalyst can vary depending on, for example, the amount of catalyst desired. For example, and by way of example only, about 45.4 kg of chromic acid can be combined with about 1.81 kg of potassium dichromate to form a chromium-alkali solution and then mixed with about 100 g of activated carbon.

  The next four examples are typical of the preparation of catalyst compositions.

Example 1
The acid composition solution A can be prepared by dissolving 3000 g of CrO 3 (chromium oxide (VI)) in 2222 g of pure water. The acid composition solution can be mixed in a Nalgene® container equipped with a spigot and magnetic stirring. The alkali metal composition solution B can be prepared by adding 166.7 g of K ₂ CrO ₇ (potassium dichromate) to 4167 g of pure water. The alkali metal solution can be placed in a second Nalgene container equipped with a spigot and magnetic stirring for mixing. To ensure dissolution of all compositions in the solvent, the amount of solvent can be analyzed for metals such as chromium and potassium. Solution A can then be added to Solution B and further mixed if deemed appropriate for the composition of the chromium-alkali solution. Substantially lined with fluororesin such as Kynar (R) (Arkema, 4-8 cours Michelet, la Defense 10, F92091 Paris la Defense Cedex) with polypropylene ports and plugs and stainless steel gauges and valve fittings The tumbler device can be loaded with 8333 g of activated carbon (Takeda, coconut shell, pelletized). The tumbler device can be sealed by bolting the flange in place. Solution (A + B) can be injected through a port from a spigot in a Nalgen container.

  When a chromium-alkali solution is added to carbon to form a catalyst solution, water vapor released from the solution is observed. After all the chromium-alkali solution has been added to the carbon, the tumbler device is plugged and the vapor pressure is released through a valve, allowing the pressure in the tumbler device to be maintained at about 136-143 kPa. The catalyst solution mixes in the tumbler apparatus for about 5 minutes and generates significant vapor products. When mixing is complete, the catalyst composition is observed to release steam, but may be essentially dry.

Example 2
The process of Example 1 can be repeated using Calgon (coconut shell, flake) carbon. The generated steam can have a light orange color.

Example 3
The acid composition solution A can be prepared by dissolving 72 g of CrO ₃ (chromium oxide (VI)) in 53.3 g of pure water. The acid composition solution can be mixed in a Nalgene container equipped with a spigot and magnetic stirring. The alkali metal composition solution B can be prepared by adding 4 g of K ₂ CrO ₇ (potassium dichromate) to 100 g of pure water. The alkali metal solution can be placed in a second Nalgene container equipped with a spigot and magnetic stirring for mixing. To ensure dissolution of all compositions in the solvent, the amount of solvent can be analyzed for metals such as chromium and potassium. Solution A can then be added to Solution B and further mixed if deemed appropriate for the composition of the chromium-alkali solution.

  A tumbler device substantially lined with a fluororesin such as Kynar equipped with a polypropylene port and plug, and a stainless steel gauge and valve fitting, can carry 200 g of activated carbon (Takeda, coconut shell, pelletized). The tumbler device can be sealed by bolting the flange in place. Solution (A + B) can be injected through a port from a spigot of Nalgen containers.

  When a chromium-alkali solution is added to carbon to form a catalyst solution, water vapor released from the solution is observed. After all the chromium-alkali solution has been added to the carbon, the tumbler device is capped and the vapor pressure is released via the Whitney valve, and the pressure in the tumbler device can be maintained at about 136-143 kPa. The catalyst solution mixes in the tumbler apparatus for about 4 minutes and generates significant vapor products. When mixing is complete, the catalyst composition is observed to release steam, but may be essentially dry.

Example 4
The chromium-alkali solution can be made by dissolving 360 g CrO ₃ (chromium oxide (IV)) and 20.0 g K ₂ CrO ₇ in 650 g pure water in a 1 liter plastic solution.

  Then, a chromium-alkali solution can be added to a vessel having 1000 g Takeda activated carbon to form a catalyst solution. The catalyst solution can be mixed and the solvent can be removed using the exotherm associated with mixing. After mixing for about 2 hours, if little heat is released from the container, the container has a catalyst composition that is essentially free of solvent.

  Referring again to the system 10, the catalyst composition 20 can be mounted in the reactor 12 and constitute a solid matrix contained within the reactor 12. Prior to use to catalyze the reaction between the reactants in the reactant container 14 and the reagents in the reagent container 16, the catalyst composition 20 can be made and activated. For example, and by way of example only, reactor 12 is heated to about 250 ° C. and a stream of inert gas such as nitrogen at about 5 liters / minute is fed through reactor 12. After passing through the reactor 12, the moisture content of the nitrogen is monitored and, for example, if the moisture content is sufficiently low, such as below the ppm level, the catalyst is deemed to be sufficiently dry and found to be useful for the reaction.

According to a typical implementation, the catalyst composition 20 can be activated and made for use with a given reagent. For example, the catalyst composition 20 can be provided in the reactor 12. According to a typical implementation, the composition 20 can be completely filled inside the reactor 12. The reactor 12 can be heated to provide heat to the composition 20, and the reactor 12 can be provided with a dry composition such as an inert gas. According to a typical implementation, reactor 12 with heated composition 20 therein can be provided with N in the form of N ₂ . As the dry composition is provided to the reactor 12, the effluent from the reactor 12 can be monitored for water. When the water in the effluent reaches a predetermined level, the supply of the dry composition can be stopped and the supply of the activated composition to the reactor 12 can be started. The activation composition can have a halogenating reagent such as HF as described herein, but can also have other halogenating reagents such as HBr and HCl, depending on the desired product.

According to a typical implementation, an activation composition such as HF can be provided to a catalyst composition having Cr and O, such as a catalyst composition made from a CrO ₃ solution described herein. In providing the activation composition to the catalyst composition, the effluent from the reactor 12 can be monitored for water. When water or HF in the effluent reaches a predetermined level, it is considered that the supply of the activation composition was stopped and the catalyst composition was activated or produced.

As another example of activation and preparation of the catalyst composition 20, the reagent in the reagent container 16 has a halogenating reagent such as a combination of hydrofluoric acid, for example, hydrogen fluoride, an inert gas, and in a predetermined embodiment, An oxidizing agent such as oxygen from the reagent container 22 is provided to the catalyst composition via the reactor, and the catalyst composition for use and the activation of the catalyst composition can be performed. For example, and by way of example only, the reactor is heated to about 380 ° C. and about 0.6 g / min HF, 0.9 g / min N 2 and 0.1 g / min through the catalyst composition for about 12 hours. O ₂ in minutes can be supplied. Prior to contacting the catalyst composition with the reactants, the reactor can be cooled to the temperature utilized for the reaction. Examples 5 and 6 below are typical of catalyst composition activation.

Example 5
About 2400 g of catalyst composition can be charged to the reactor (the tube has a volume of 2832 cc). The catalyst composition is dried under nitrogen, heated to 100 ° C, held at about 100 ° C for 30 minutes to maintain equilibrium, and increased to about 150 ° C, about 175 ° C, about 200 ° C, and about 250 ° C. And maintain an equilibrium state for 30 minutes at that temperature. Total drying time may range from about 3 to 8 hours. Once the catalyst is dry (no water vapor released from the reactor is detected), an HF flow is started and the reactor temperature is increased to about 300 ° C. HF can be passed through the reactor until HF breakthrough is detected. HF is fed at 5 g / min, giving a contact time of 14.5 seconds with 900 g of HF being fed, which is about 0.375 g HF for 1 g of catalyst.

Example 6
An industrial hot oil reactor can be charged with about 69.5 g of the catalyst composition. To dry the catalyst bed, the reactor can be provided with a nitrogen purge of 150 cc / min of nitrogen. The reactor can be maintained at 100 ° C., raised from 100 ° C. to 343 ° C., and maintained for more than 7 hours until no vapor released from the reactor is detected. Then, HF can be provided to the reactor for 1 hour at a flow rate of 383.4 cc / min before starting the reactants.

  According to an exemplary embodiment, the compound or reactant from the reactant container 14 can be contacted with the reagent from the reagent container 16 in the presence of the catalyst composition 20. According to an exemplary embodiment, the reactant in reactant vessel 14 may be a C-3 compound, and in an exemplary embodiment, the C-3 compound may have at least one halogen. One halogen may be, for example, one or more of F, Cl, Br, and I. The C-3 compound can further have, for example, H. According to an exemplary embodiment, the C-3 compound is 1,1,1,3-tetrachloropropane (tetrachloropropane, TCP). Other C-3 compounds can be reacted using a catalyst compound, but the geminal carbon is not equipped with a halogen, the C-3 compound having a halogen at both ends is exchanged with a halogen, and the halogen is removed. It is shown to constitute a halogenated olefin such as a reaction of chloropropane and to constitute 3,3,3-trifluoroprop-1-ene (trifluoropropene, TFP) in the presence of the catalyst composition 20.

  Referring to the reagent in reagent container 16, the reagent can have at least one halogen, and the halogen can have one or more of F, Cl, Br, and I. The reagent can also have hydrogen, for example. A typical reagent, sometimes referred to as a halogenating reagent, can have HX, where X is one of F, Cl, Br, and I. According to an exemplary embodiment, the catalyst composition 20 may have at least one alkali metal when contacting the C-3 compound and the reagent in the reagent container 16. Contacting the C-3 compound with the reagent in reagent container 16 can occur in reactor 12 configured to maintain the temperature of the catalyst composition in the reaction chamber at least about 250 ° C. according to an exemplary embodiment. . According to another embodiment, the temperature of the catalyst composition in the reaction chamber can be maintained below about 350 ° C., and in yet another embodiment the catalyst composition in the reaction chamber while contacting the C-3 compound with the reagent. The temperature of the object can be maintained at about 300-330 ° C.

  The exemplary system 10 can have an oxidizing reagent container 22. According to an exemplary embodiment, an oxidation reagent can be provided to the reaction chamber while the reactant-bearing compound is in contact with the reagent in reagent container 16. The oxidizing reagent can have oxygen in the form of O2, for example.

  According to an exemplary embodiment, reagent container 16 can have reagent HF. The reactant container 14 can have tetrachloropropane as a reaction compound, and the oxidizing reagent container 22 can have oxygen as an oxidizing reagent. Oxygen may be at least about 0.1-0.3% of the molar amount of both the C-3 compound and the reagent when provided to the reactor 12. Tetrachloropropane can be provided from a short chain polymerization reaction such as a short chain polymerization of carbon tetrachloride and ethylene. According to a typical embodiment, HF can be fed through an 836 liter reactor at about 10.6 kg / min. Tetrachloropropane can be fed through the reactor at about 5.37 kg / min and oxygen can be fed through the reactor at about 0.03 kg / min. According to exemplary embodiments, contact of these reactants and reagents with catalyst composition 20 can result in the formation of trifluoropropene, or in particular, 1,1,1-trifluoropropene. This trifluoropropene is provided to the product container 18 along with one or more of the reactants, reagents, or by-products. The product container 18 can be connected to a typical product purification device, such as one or more distillation, washing, or drying devices known to those skilled in the art.

  According to another exemplary embodiment, the reactant in the reactant vessel 14 can have a C-1 compound, the C-1 compound can have at least one halogen, and the halogen can be, for example, F, Cl, Br, and I may be used. The C-1 compound in the reactant container 14 can also have H, for example. In an exemplary embodiment, the C-1 compound may be dichloromethane. The reagent in the reagent container 16 may be HF, for example. According to an exemplary embodiment, dichloromethane from reactant vessel 14 can be contacted with the catalyst composition in the presence of reagents in reagent vessel 16. In an exemplary embodiment, the reagent in reagent container 16 may be, for example, HF. In a reactor with an internal volume of about 2158 liters, dichloromethane is provided at about 10.8 kg / min and HF is provided at about 40.8 kg / min. The contact of dichloromethane with HF occurs in the presence of an oxidizing reagent, and the oxidizing agent may be less than about 0.3% mole fraction of the reactants. Contacting dichloromethane with HF is performed while maintaining the catalyst composition at a temperature of at least about 316 ° C. in a typical embodiment. In other embodiments, when the dichloromethane is contacted with HF, the catalyst composition in the reaction chamber is maintained at less than about 343 ° C, and in yet other embodiments, the catalyst composition is maintained at about 316-341 ° C. .

  According to an exemplary embodiment, contacting dichloromethane with reagent HF can result in the formation of difluoromethane. Difluoromethane is efficiently produced from dichloromethane and can result in very little intermediate products such as fluorochloromethane and unreacted materials such as dichloromethane. Difluoromethane is provided in a product container 18, which may take the form of or be connected to a purification device such as, for example, one or more devices for distillation, washing or drying.

  If the catalyst composition 20 is used for an extended period of time, the catalyst composition can also be reactivated. For example, an oxidizing agent can be provided to the catalyst composition without providing reactants to the reactor 12. According to a typical implementation, the catalyst composition can be heated to a predetermined temperature and an oxidizing agent can be provided to the composition for a predetermined time. After this time is complete, the catalyst composition 20 is contacted, for example, with a halogenating reagent as described herein until it is determined that the predetermined compound is at the predetermined level in the effluent.

  As another example, the reagent can be provided to the catalyst composition in the presence of an inert gas such as nitrogen and an oxidizing agent without providing a reactive compound. In a typical example, an 836 liter reactor is heated to about 3.6 kg / min HF, 2.9 kg / min N 2, and about 0.12 kg / min O 2 while the reactor is heated to a predetermined temperature. Can provide.

  Depending on the production system having the catalyst composition 20 and configured as described herein, the product can be produced for extended periods of time. For example, and by way of example only, 24 hours a day, 7 days a week, depending on the production of TFP, the catalyst composition for several weeks at a time without reactivation or replacement of the catalyst composition 20 In the presence of the product 20, TFP can be produced from TCP and HF. When reactivating the catalyst composition 20, it can be produced several months at a time, even up to six months at a time, operating 24 hours a day, 7 days a week.

  As another example, and by way of example only, the production of difluoromethane from the reaction of dichloromethane and HF in the presence of catalyst composition 20 can be achieved without reactivation or replacement of catalyst composition 20 for one day. You can rely 24 hours a day, 7 days a week, several months at a time, and even one year completely continuously. As an example, using only 136 kg of catalyst composition 20, about 600,000 kg of difluoromethane can be produced.

The drawing is a schematic diagram of a system according to an exemplary embodiment of an exemplary embodiment of the present invention.

Claims (46)

A base,
At least about 13% (by weight) chromium;
At least one alkali metal,
A catalyst composition comprising:   The catalyst composition according to claim 1, wherein the base comprises activated carbon.   The catalyst composition according to claim 1, wherein the one kind of alkali metal contains potassium.   The catalyst composition according to claim 1, wherein the base contains activated carbon, and the alkali metal is potassium.   The catalyst composition of claim 1, wherein the molar ratio of chromium to one alkali metal is at least about 50: 1. Producing a first solution containing an alkali metal composition comprising K ₂ CrO ₇ ;
Making the second solution by contacting the first solution with a base;
The second solution contains the base and an alkali metal, and the catalyst composition containing the alkali metal composition and the base is removed from the second solution . The manufacturing process according to claim 6, wherein the first solution contains water . The manufacturing process according to claim 6, wherein the base contains activated carbon . The second solution further comprises water, and removal of the catalyst composition from the second solution comprises separating at least a portion of the water of the second solution from the alkali metal composition and the base. The manufacturing process according to claim 6. The manufacturing process according to claim 9 , wherein a part of the water to be separated is a large part of the water. The manufacturing process according to claim 10 , wherein a part of the water to be separated is substantially all water. A manufacturing process comprising contacting an at least partially halogenated compound with a reagent in the presence of a catalyst composition comprising:
The catalyst composition comprises a base, chromium, and at least one alkali metal. Contacting a compound with a reagent in the presence of a catalyst composition comprises
Providing a reaction chamber containing the catalyst composition and configured to receive both compounds and reagents;
13. The manufacturing process of claim 12, further comprising supplying oxygen to the reaction chamber during the contacting. The manufacturing process of claim 12 , wherein oxygen is provided to the chamber by an amount that is at least about 0.1% of the molar amount of both the compound and the reagent. The production process according to claim 12 , wherein the compound is a C-3 compound . 16. The production process according to claim 15, wherein the halogen of the C-3 compound is one of F, Cl, Br, and I. The process according to claim 16, wherein the C-3 compound contains H. The production process according to claim 17, wherein the C-3 compound is 1,1,1,3-tetrachloropropane. The production process according to claim 12 , wherein the compound is a C-1 compound. Contacting a compound with a reagent in the presence of a catalyst composition comprises
Providing a reaction chamber containing the catalyst composition and configured to receive both the compound and the reagent;
20. The process of claim 19, further comprising supplying oxygen to the reaction chamber during contact. 21. The manufacturing process of claim 20 , wherein oxygen is provided to the chamber by an amount that is at least about 0.1% of the molar amount of both the compound and the reagent. 21. The manufacturing process according to claim 20 , wherein the halogen of the C-1 compound is one of F, Cl, Br, and I. The manufacturing process according to claim 22, wherein the C-1 compound contains H. The process according to claim 23, wherein the C-1 compound is dichloromethane. Contacting the C-1 compound with the reagent in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-1 compound and the reagent;
Maintaining the temperature of the catalyst in the reaction chamber at least about 316 ° C .;
25. The manufacturing process of claim 24 , comprising providing both the C-1 compound and a reagent in a reaction chamber. Contacting the C-1 compound with the reagent in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-1 compound and a reagent;
Maintaining the temperature of the catalyst in the reaction chamber below about 343 ° C .;
25. The manufacturing process of claim 24, wherein both the C-1 compound and the reagent are provided in a reaction chamber. Contacting the C-1 compound with the reagent in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-1 compound and a reagent;
Maintaining the temperature of the catalyst in the reaction chamber at about 316-341 ° C .;
25. The manufacturing process of claim 24, wherein both the C-1 compound and the reagent are provided in a reaction chamber. 29. A process according to claim 28, wherein the reagent comprises at least one halogen. 29. The process of claim 28 , wherein the at least one halogen is one of F, Cl, Br, and I. 30. The manufacturing process according to claim 29, wherein the reagent contains H. The manufacturing process according to claim 30 , wherein the reagent contains HX, and X is one of F, Cl, Br, and I. The manufacturing process according to claim 12, wherein the base contains activated carbon. The manufacturing process according to claim 12 , wherein the one alkali metal is potassium. The process of claim 12, wherein the molar ratio of chromium to one alkali metal of the catalyst composition is at least about 50: 1. A manufacturing process comprising contacting an at least partially halogenated C-3 compound with a reagent in the presence of a catalyst composition, the catalyst composition comprising at least one alkali metal Manufacturing process. Contacting the reagent with a C-3 compound in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-3 compound and a reagent;
Maintaining the temperature of the catalyst in the reaction chamber at least about 300 ° C .;
36. The manufacturing process of claim 35, wherein both the C-3 compound and the reagent are provided in a reaction chamber. Contacting the reagent with a C-3 compound in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-3 compound and a reagent;
Maintaining the temperature of the catalyst in the reaction chamber below about 350 ° C .;
36. The manufacturing process of claim 35 , comprising providing both the C-3 compound and a reagent in a reaction chamber. Contacting the reagent with a C-3 compound in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-3 compound and a reagent;
Maintaining the temperature of the catalyst in the reaction chamber at about 300-330 ° C .;
36. The manufacturing process of claim 35, wherein both the C-3 compound and the reagent are provided in a reaction chamber. Contacting the reagent with a C-3 compound in the presence of the catalyst composition comprises:
Providing a reaction chamber containing the catalyst composition and configured to receive both the C-3 compound and a reagent;
36. The process of claim 35, further comprising supplying oxygen to the reaction chamber during contact. 40. The manufacturing process of claim 39 , wherein oxygen is supplied to the chamber by an amount that is at least about 0.1% of the molar amount of both the C-3 compound and the reagent. A manufacturing system having a reactor connected to both a reactant container and a reagent container,
The reactor contains a catalyst composition comprising at least about 13% (by weight) chromium and at least one alkali metal. 42. The manufacturing system according to claim 41, wherein the catalyst composition further contains a base. 42. The manufacturing system according to claim 41, wherein the base includes activated carbon. 44. The manufacturing system according to claim 43, wherein one alkali metal is potassium. 42. The manufacturing system according to claim 41, wherein the reactor is further connected to an oxidant vessel. 42. The manufacturing system according to claim 41, wherein one alkali metal is potassium.

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