text:
|Publication number
|Publication type
|Application number
|Publication date
|Jun 6, 2006
|Filing date
|May 24, 2000
|Priority date
|Feb 3, 2000
|Fee status
|Publication number
|Thomas Schwalbe, Sebastian Oberbeck, Klaus Golbig, Michael Hohmann, Andreas Oberbeck
|Original Assignee
|Cellular Process Chemistry, Inc.
|Export Citation
|BiBTeX, EndNote, RefMan
|Patent Citations (41), Non-Patent Citations (1), Referenced by (35), Classifications (29), Legal Events (5)
|External Links: USPTO, USPTO Assignment, Espacenet
This application is a continuation-in-part (CIP) of a patent application Ser. No. 09/496,999, filed on Feb. 3, 2000, which is now issued as U.S. Pat. No. 6,537,506, the benefit of the filing date of which is hereby claimed under 35 U.S.C. � 120.
This invention generally relates to a modular chemical production system, and more specifically, to a miniaturized modular chemical production system that incorporates a microreactor, and which enables modules to be added or removed from the system to accommodate the type and quantity of chemical produced thereby.
Methods of controlling and optimizing the production of chemical substances are well known. The control of parameters such as temperature, pressure, mixing conditions, relative volumes of the reactants, and the use of catalysts are generally well understood. Recently, much attention has been directed to the use of micro-scale reactors for both development and production of chemical products. These types of microreactors offer several clear advantages over more conventional macro-scale chemical production systems.
First, the control of chemical processes within very small reactors is much simpler than the control of the same process in a large-scale production tank. Safety is enhanced, as relatively small volumes of chemicals are processed within a single reactor. Thus, the severity of any potential accident involving a single microreactor is minimized. Once a reaction process has been developed and optimized in a microreactor, production in larger quantities can be enabled by replicating the microreactors in sufficient quantity so as to achieve the required production levels. If such reactors can be fabricated in quantity, and for a modest cost, industrial quantities of a desired product can be manufactured with a capital expenditure equal to or even less than that of a traditional chemical production facility.
This approach also offers a substantial improvement over conventional methods for moving from small-scale production to large-scale production. In the past, a chemical production process perfected in the laboratory using small volumes of chemicals often required considerable modifications to be made in the process when converting it to large-scale production, due to changes in process conditions. Such scale-up problems often cause frustrating and expensive delays in moving from research to production.
The pharmaceutical industry in particular engages in chemical research on many new chemical compounds every year, hoping to find a drug or chemical compound with desirable and commercially valuable properties. The research process is complicated, time-consuming, and costly. Discovering a new drug has been likened to searching for the proverbial needle in a haystack. Literally tens of thousands, and sometimes hundreds of thousands, of chemical compounds must be made and tested to find one that can achieve a beneficial result without prohibitive side effects.
Such a complicated process costs vast amounts of time and money. The Food and Drug Administration (FDA) estimates that, on average, it takes eight-and-a-half years to study and test a new drug before the agency can approve it for the general public. Drug companies spend $359 million, on average, to develop a new drug, according to a 1993 report by the Congressional Office of Technology Assessment. A company such as Hoffmann-La Roche, whose annual sales in the United States alone are about $3 billion, spends about $1 billion a year on research worldwide.
It has been recognized that microreactors are of tremendous potential use to the pharmaceutical industry. Aside from providing safety benefits, and providing the ability to ease the transition from research to full-scale commercial production, microreactors utilize small volumes of chemicals efficiently. Often the chemicals used in drug research are costly and unavailable in significant quantity. Thus, the ability to perform research using small volumes of chemicals efficiently is important.
It has further been recognized that end users of microreactors, whether in a research setting or a production setting, desire not just a microreactor, but an integrated system that enables an end user to easily and effectively exploit the full potential of microreactors. Just as many computer users purchase a complete computer system, rather than just the microprocessor, which is at the heart of a computer system, many research and production facilities will desire to purchase a microreactor system that enables the end user to efficiently produce a variety of desired chemicals in almost any desired quantity, by making changes in the system, to scale the production as appropriate.
At least one design for such an integrated microreactor based system has been investigated. A patent issued to Bard (U.S. Pat. No. 5,580,523) describes a modular microreactor that includes a series of reactor modules connected in fluid communication, each reactor module having a particular function. Bard specifically teaches that the plurality of microreactor modules are mounted laterally on a support structure, and that individual microreactor modules can be replaced as needed. These reactor modules disclosed in the Bard patent minimally include a reactor module, a separator module, and an analyzer module, and additional microreactor modules can be added in series or parallel. Bard specifically teaches that separate mixing modules and reaction volume modules are used. This patent also teaches that a variety of generic components, such as computerized controls, pumps, valves, flow channels and manifolds can be included in such an apparatus.
It would be desirable to provide a modular chemical production system that utilizes microreactors but offers additional flexibility to the user, beyond that of the Bard system. For example, it would be desirable for all of the components of the system, and not just the microreactor units, to be modular in design so that any component, such as a pumping unit, can be replaced as needed to produce either a different type of chemical product, or a different quantity of the desired chemical product, or to easily replace a defective component.
Furthermore, to reduce the number of modules required, it would be desirable to provide a reaction module in which the mixing of the chemicals reacting to form the desired chemical product is achieved within the same reaction module in which the chemical reaction between these chemicals occurs, so that a separate mixing module is not required. It would also be desirable for such a single reaction module to incorporate a microreactor that enables rapid diffusion mixing. Diffusion mixing can be achieved by forcing fluids to flow in a laminar flow pattern within small fluid channels and is characterized by being extremely rapid and efficient, more so than mixing achieved by creating turbulence or agitation. It would further be desirable to provide a reaction module in which the microreactor is replaceable, so that a different type of chemical product can be produced without requiring the replacement of the entire reaction module.
Another desirable feature of the microreactor modular system is a control module that includes an intuitive user interface, enabling a user to select from a stored menu of desired chemical products, so that after selecting a desired amount of a particular product, the user is only required to connect the system to a source of the required chemicals, and the control unit will control the system according to stored processing parameters, such as flow rates, temperature, and pressure, to produce the selected product.
A pump module in such a system should provide sufficient pumping capacity so that flow rates of reactants into the reaction module can be increased to the maximum capacity of the reaction module without requiring replacement of the pump module with a higher rated output pump module. However, should additional reaction modules be necessary within a system to further increase the quantity of product produced, the pump module should be configured to be readily replaced with a pump module capable of providing the required flow rate.
It would further be desirable for all the processing modules to have housings of a consistent size and shape. Any inlet and outlet ports incorporated into the housings of the processing modules should be located in the same positions on all the processing modules, and all connections between processing modules should be of a quick connect type to enable the rapid replacement or addition of processing modules when changing the configuration of the system. Such connections should preferably be self closing to prevent spills when processing modules are replaced. The user should have an option to select processing modules adapted for either parallel fluidic heat transfer or serial fluidic heat transfer, when temperature control of a chemical process is required.
Because many possible reactions that can be beneficially achieved using such a modular chemical production system involve pressure dependent reactions, it would also be desirable for such a system to include a throttle, such as a proportional valve, at the end of the reaction path. Closing the throttle will make the pumps in the pump module apply a higher pressure to the liquids, to maintain a constant flow rate.
In accord with the present invention, a modular system is defined for producing a desired chemical product from a plurality of reactants. The reactor system includes a control module and a reaction module. Different chemical products can be produced by replacing the reaction module or reconfiguring the modular system, as appropriate.
The control module is adapted to monitor and control a production of the desired chemical product by controlling the flow of each reactant from a reactant supply source. The control module includes a memory, a processor, and a user interface. Stored in the memory are machine instructions that are executed by the processor to enable the control module to carry out its control functions. The control module also controls a reaction module that is in fluid communication with each reactant supply source and which includes a microreactor in which the desired chemical product is produced by a reaction between the reactants. The microreactor includes a mixing volume and a reaction volume. The plurality of reactants are preferably fluids, and may be in a gaseous state.
In one embodiment, the modular system includes a pump module, which is also controlled by the control module. The pump module is in fluid communication with each reactant supply source, and with the reaction module and enables and controls the flow of fluids within the modular system under the direction of the control module.
Optionally, an additional processing module can be included in fluid communication with the reaction module. In one embodiment, the additional processing module comprises a residence time module that includes a capillary passage of a selected length, the length controlling a residence time of the desired chemical product in the residence time module. Preferably, the residence time module also includes a proportional valve that is controllably connected to the control module to enable the control module to selectively vary a pressure within the modular system.
The modular system can also include additional reaction modules, each including a microreactor, and each microreactor is designed to achieve a single step in a multi-step reaction. A chemical product that can be made by carrying out two different processing steps can be produced using a modular system in accord with the present invention that incorporates two reaction modules, each reaction module including a microreactor adapted to facilitate a single step in the two step process. Each reaction module will be controllably connected to the control module. Fluid from each reactant supply source will be directed through the pump module (unless no pump modules is used, as can be the case when the reactants are gases) and into a first reaction module, in which the first step in the reaction is achieved. The second reaction module is in fluid communication with the outlet of the first reaction module, and the partially reacted fluids will flow from the first reaction module to the second reaction module, where the second step in the reaction will be achieved. If required, residence time modules can be placed between the first and second reaction modules. In a similar fashion, reactions requiring more than two steps can be achieved using a corresponding number of reaction modules. The microreactors are configured to facilitate the completion of a specific class of chemical reactions, and each microreactor can be removed from its reaction module and replaced with a different microreactor configured to facilitate the completion of a different chemical reaction, thus enabling the system to selectively complete a variety of different chemical reactions, thereby producing a wide variety of different chemical products.
Furthermore, the each microreactor is configured to enable at least one process relating to the production of a desired chemical product. Frequently microreactors will enable a plurality of reagents to be mixed together to form a desired product. It is preferred that each microreactor be able to achieve a precise temperature control of the plurality of reagents and the product within the microreactor. Each microreactor will be designed to facilitate a particular type of chemical reaction, such as a liquid/liquid reaction, a gas/liquid reaction, or a gas/gas reaction. It is envisioned that microreactors enabling additional processes relating to the chemical reaction will be useful. Such microreactors can be achieved by incorporating various types of features relating to the reaction process. In addition to enabling control of the temperature within the microreactor, such features are likely to include enabling processes such as diffusion based mixing, catalytic based processing, and/or providing and manipulating one or more of the following: a source of electromagnetic radiation, a source of sonic radiation, a source of alpha radiation, a source of beta radiation, a source of gamma radiation, a source of X-ray's, a source of radioactive particles, a source of charged particles, a source of light, an electric field, and a magnetic field. Thus, a system including a replaceable microreactor is suitable for facilitating the production of a wide variety of different chemical products. By providing a plurality of different microreactors, each of which is adapted to process a different class of reactions (such as liquid/liquid reactions), the resulting system will enable at least one process, and optionally, will enable additional processes, such as temperature control. The flexibility of such a system enables a user to selectively produce a desired product, by selecting a microreactor incorporating features appropriate for the function. While a wide variety of microreactors, each incorporating specialized features, can be fabricated, it is expected that a liquid/liquid type microreactor, incorporating only temperature control and mixing features, can be beneficially employed to produce a substantial variety of desirable chemical products.
Preferably the reaction module includes a housing with a first side that has a plurality of ports. One port enables the reaction module to be controllably connected to the control module and other ports enable it to be in fluid communication with each reactant supply. A second side of the housing includes a plurality of ports that enable the reaction module to be connected in fluid communication with the additional processing module or with a product reservoir. Also included in the housing is a mounting frame for the microreactor. The reaction module includes means for promoting the production of the desired chemical product, such as a temperature sensor, a mixing volume in which a stacked laminar flow of said plurality of reactants is enabled, and a reaction volume.
The modular system includes a plurality of fluid paths, including a fluid path for each of the plurality of reactants, a fluid path for the desired product, at least one fluid path for heat transfer media, and at least one fluid path for spent heat transfer media. The heat transfer media fluid paths can be configured in one of a parallel fluidic system and a serial fluidic system.
The pump module includes at least one pump that is controllably connected to the control module. The pump is in fluid communication with both a heat transfer media fluid supply and the reaction module. Or, the pump is in fluid communication with at least one of the plurality of reactants, and the reaction module. In one embodiment, the pump module includes an individual pump for each of the plurality of reactants, each individual pump being in fluid communication with a supply of a different one of the plurality of reactants, and with the reaction module. The pump module further preferably includes valves controllably connected to the control module, for controlling the flow of the plurality of reactants to the reaction module. In one embodiment, the pump module also includes a filter for each reactant, to remove undesired material from the plurality of reactants before the reactants flow to the reaction module.
Preferably, the pump module includes a housing having a first side that includes a plurality of ports adapted to enable the pump module to be controllably connected to the control module and to be in fluid communication with each reactant supply, and a second side that includes a plurality of ports adapted to enable the pump module to be in fluid communication with the reaction module. In addition, all connections between modules are preferably achieved using quick connect type connectors that enable rapid connection and disconnection of the modules.
Another aspect of the present invention is directed to a modular system adapted for producing a desired chemical product using only a single reactant, rather than a plurality of reactants. In such a modular system the reactor module will facilitate a single component reaction, for example, photochemically or pyrolytically. The modular system includes elements that are generally consistent with the elements of the modular system described above. Yet another aspect of the present invention is directed to a method for producing a desired chemical product with a modular system. The method includes steps that are generally consistent with the functions of the modular system described above.
Another aspect of the present invention is a microreactor for use in the modular reaction system, for reacting one chemical with at least one other chemical, for the purpose of forming a chemical product. The reactor includes a plurality of simple plates, each simple plate having at least one opening formed therein, the simple plates being stacked together to form a plurality of layers and arranges so that at least one opening in each simple plate overlaps at least one other opening in an adjacent simple plate, thereby forming at least one pathway between at least some of the layers.
Preferably, openings within different layers align so as to form at least one inlet port and at least one outlet port, for the receipt and discharge of chemicals, and to form at least one pathway for conveying chemicals to be processed. At least one pathway is formed that is in fluid connection with the inlet and outlet ports, and each simple plate has at least one opening formed in it.
A material from which the simple plates are fabricated is selected for compatibility with the chemical process. In one embodiment, the simple plates are formed from a material selected from the group consisting of crystalline wafers, ceramics, glasses, polymers, composite materials, and metals. Preferably, if formed from a metal, stainless steel is used. The material of the crystalline wafer is selected from the group consisting of silicon and germanium.
It is also preferable that the reactor accommodate a plurality of operations, including temperature control, control of chemical residence time, chemical mixing, and chemical reacting. Temperature control is achieved using a combination of one or more temperature sensors and one or more heat exchangers. Preferably, chemical mixing is carried out by employing pathways sized so that a reactant achieves a stacked laminar flow with respect to at least one other reactant.
In a reactor adapted for processing at least two reactants to form a desired chemical product, an inlet opening for each of the reactants and an outlet opening for the chemical product is provided in at least one of two outer simple plates. An intermediate simple plate is included for mixing the reactants and has at least one opening in fluid communication with each inlet opening and the outlet opening.
Generally, at least one heat transfer fluid inlet port is included in at least one of the outer simple plates, so that at least one heat transfer fluid can be introduced into the chemical reactor. Each heat exchanger is defined by an opening in a different intermediate simple plate. The opening is in fluid communication with the heat transfer fluid inlet and outlet ports and is disposed between adjacent simple plates.
Preferably, each heat exchanger is used to modify the temperature of at least one of the reactants and/or the chemical product. The heat exchangers can be used to modify a temperature of one of two reactants such that they are at different temperatures.
The thickness of the outer simple plates is about 3 millimeters, and that of the plurality of intermediate simple plates is at least about 0.2 millimeters, but not more than about 0.6 millimeters.
Preferably, when the thickness of the intermediate simple plates that are adjacent to a heat exchanger is about 0.3 millimeters. When a series of openings in the simple plates of the chemical reactor defines a fluid path for a heat transfer fluid that flow through more than one heat exchanger, the flow rate and fluid pressure of the heat transfer fluid within each such heat exchanger are substantially.
The foregoing aspects and many of the attendant advantages of this invention will become more readily appreciated as the same becomes better understood by reference to the following detailed description, when taken in conjunction with the accompanying drawings, wherein:
In accord with the present invention, a modular system is defined for producing a chemical product from a plurality of reactants and includes a plurality of replaceable modular units. A control module enables automated control of parameters such as concentration, flow rates, temperature, pressure, pH values, and residence time. The system is configured for continuous operation and in its simplest form, can be used in chemical research facilities for the continuous production of small volumes of specialty chemicals required for research applications. Individual modules can be replaced to modify the performance of the system, and reaction modules can be replaced with reaction modules having a different configuration to enable the completion of different classes or types of reactions. Furthermore, a single reaction module is preferably capable of facilitating a plurality of processes relating to the production of a desired product from a plurality of reagents, and the system enables a user to select from those plurality of processes which processes are appropriate to produce a desired product from a given set of reagents. Also, the reactor portion of the reaction module can be removed and replaced with a reaction module optimized for a particular class of reactions (such as liquid/liquid reactions). Reactors optimized for a particular class of reactions can be further optimized to enable different processes related to completing a reaction to be facilitated, such as diffusion based mixing, and temperature control.
It should be noted that such a system can be adapted to facilitate reactions requiring only a single reactant, rather than a plurality of reactants. Many such reactions are possible, and frequently involve reacting a single component photochemically or pyrolytically. For example, to facilitate a single component reaction of the photochemical type, the reactor portion of the reaction module will be optimized for photochemical reactions. It should therefore be understood that while the preferred embodiment described below references a modular system optimized for producing a desired product from a plurality of reactants, the scope of the invention is intended to encompass modular systems optimized to facilitate the production of a desired product by reacting only a single reactant.
Control module 12 is connected to control pump module 14, reaction module 18, any additional process modules 20, and fluid supply source 16. Reactants and heat transfer media flow from fluid supply source 16 to the pump module. Control module 12 controls the flow of fluids from fluid supply source 16, as well as controlling the pumping rate of pump module 14. Heat transfer media and reactants flow from pump module 14 to reaction module 18, where the desired chemical reaction takes place, and the desired product is produced. The product exits reaction module 18 and flows either to one or more additional process modules 20, or to a product collection vessel 22.
Additional process modules 20 can carry out a variety of functions. In one embodiment, the additional process module comprises a residence time chamber to provide additional time for the reagents to complete their reaction before the product they produce is collected at product recovery vessel 22. Depending on the nature of the desired product, and the chemical process used to produce that product, additional process module 20 can comprise an additional reaction module 18, for example, as would be required for a two-step reaction process in which the product of the first reaction module 20 is combined with a reagent to produce the final desired product.
Reactant gas supply 16 a and heat transfer media supply 16 b are connected in fluid communication with reaction module 18. Both reactant gas supply 16 a and heat transfer media supply 16 b are controlled by control module 12, to which they are connected, and the control module adjusts the flow rates of the reactant gases by controlling valves (not separately shown) associated with the reactant gas supply. As noted above, for modest flow rates, use of a pressurized source for reactant gas supply 16 a avoids the need for a separate pump module. Standard gas bottles or commercial grade gas cylinders are expected to be useful in serving as reactant gas supply 16 a.
It is envisioned that heat transfer media supply 16 b will incorporate its own pump, which is controlled by control module 12, so that the flow rates of the heat transfer media can be controlled. In this case, the pump required to control the flow of the heat transfer media is simpler than that used in pump module 14. In
As shown in
Control module 12 is operatively connected to a Reactant 1 supply 16 c, a solvent supply 16 d, a Reactant 2 supply 16 e, and heat transfer media supply 16 b. Reactant 1 and Reactant 2 will be mixed in reaction module 18 to achieve the desired chemical product. Solvent supply 16 d is used to flush out all the fluid lines and passages in pump module 14 and subsequent modules to ensure that any reagent residue left over from previous reactions is flushed from the system and will not interfere in the current operation of the system in the present reaction. Furthermore, solvent supply 16 d can be provided at a desired temperature, in order to pre-warm or pre-chill the fluid pathways within the modular chemical reaction system.
When the system is initialized and a particular chemical product is selected from the optional reaction database within control module 12 (or the user has entered the control parameters using user interface 28), and after the user has properly placed Reactant 1 supply 16 c and Reactant 2 supply 16 e in fluid connection with pump module 14, the user employs the user interface in control module 12 to activate the system. Control module 12 is operatively connected through a data/power bus 48 to all controllable elements within pump module 14. For example, control module 12 sends a control signal to a valve 34 a, which is in fluid communication with Reactant 1 supply 16 c and solvent supply 16 d. Initially, the signal sent by control module 12 causes valve 34 a to allow solvent from solvent supply 16 d to flow through the system and flush out the fluid passages lines, as previously described. Control module 12 is similarly operatively connected through power/data bus 48 to a valve 34 b, which is in fluid communication with solvent supply 16 d and Reactant 2 supply 16 e. Again, control module 12 sends a control signal through power/data bus 48 to valve 34 b, enabling the solvent to flow to flush the fluid passages and lines within the system with solvent from solvent supply 16 d. After a desired interval has passed, control module 12 sends a signal to both valves 34 a and 34 b to shut off the flow of solvent, and to change state so as to allow the desired volumes of both Reactant 1 and Reactant 2 to flow into the system. Upon passing through valve 34 a, Reactant 1 flows through a fluid line 36 a into a pump 38, which is also operatively connected to control module 12 via power/data bus 48. Simultaneously, the desired amount of Reactant 2 flows through a fluid line 36 b to a pump 40.
Control module 12 controls the pumping rates of pumps 38 and 40 to achieve the desired flow rates of both Reactants 1 and 2. Pressure sensors 44 are included down stream of pumps 38 and 40 to provide confirmation to control module 12 that the reactants are flowing. Filters 46 are in fluid communication with fluid lines 36 a and 36 b and are employed to filter any particulate matter that may have contaminated Reactant 1 supply 16 c or Reactant 2 supply 16 e. In a preferred embodiment in which the reaction module incorporates a microreactor, these filters are particularly important. The fluid channels within the microreactor are characteristically very small in size. Thus, even relatively small particulates can clog these channels and significantly impair the efficiency of the microreactor. Preferably control module 12 is programmed to alert a user to check the filters when pressure sensors 44 indicate a change in pressure in the system, as such a pressure change may be indicative of a clogged filter. It should be noted that pressure sensors 44 and filters 46 can be disposed before pumps 38 and 40, although the preferred embodiment is as illustrated, with pressure sensors 44 disposed behind the pumps, and filters 46 disposed behind pressure sensors 44.
Control module 12 is further controllably connected to heat transfer media supply 16 b. Based on the control parameters stored within reaction database 26, control module 12 will cause heat transfer media supply 16 b to release the desired volume or control the flow rate of heat transfer media fluid through a fluid line 36 c. Fluid line 36 c is connected in fluid communication with a heat transfer media pump 42. Pump 42 is controllably connected to control module 12 to enable the flow rate of the heat transfer media fluid through the system to be controlled.
Reactant 1, Reactant 2, and the heat transfer media all exit pump module 14 and flow through fluid lines 36 a, 36 b, and 36 c, respectively, to reaction module 18. Spent heat transfer media flowing from reaction module 18 returns to pump module 14 via a fluid line 36 d. Fluid line 36 d is in fluid connection with a heat transfer media return vessel 16 f, and it should be noted that pump module 14 performs no operations on fluid line 36 d. Fluid line 36 d merely passes through the pump module to reach heat transfer media return vessel 16 f. Thus, fluid line 36 d could alternatively be routed to flow directly from reaction module 18 to heat transfer media return vessel 16 f without flowing through pump module 14. However, the modular reaction system has been designed so that all fluids used in the process flow from one module to the next, to minimize the number of fluid lines and control lines that are external to the modules.
Heat transfer media fluid enters the microreactor via heat transfer fluid line 36 c and then exits the microreactor, and the reaction module, through fluid line 36 c, which is coupled in fluid communication with any optional additional process module. If no additional process modules are included, fluid line 36 c is connected directly to spent heat transfer fluid line 36 d, which returns the spent heat transfer fluid to spent heat transfer fluid vessel 16 f.
Various different configurations of microreactors can be beneficially employed in the present invention. Each microreactor may be designed for only a specific chemical reaction, but will more likely be designed to support the production of a specific class or type of chemical products, since one design configuration is normally useable to produce various chemical products in which the reaction processes are similar in nature. A particularly useful microreactor is described in a commonly assigned co-pending U.S. patent application, U.S. Ser. No. 09/496,999, entitled "MINIATURIZED REACTION APPARATUS," which was filed Feb. 3, 2000, the specification and drawings of which are hereby specifically incorporated herein by reference. It should also be noted that while in one preferred embodiment, the reactor within reaction module 18 is a microreactor, a non-micro-scale reactor could alternatively be used in conjunction with the present invention. Microreactors are generally characterized as incorporating fluidic structures of less than 1 mm in size, especially with respect to reactant fluid pathways. Thus it should be understood that the present invention is not limited only to modular systems in which reaction modules must include a microreactor, as the reaction module can incorporate a reactor whose fluidic structures are larger in size than the microscale fluidic structures generally associated with microreactors. A reactor with larger scale fluidic structures can be used, as long as the overall size and shape of the reactor is adaptable to fit within the reaction module.
In addition to microreactors designed for only a specific chemical reaction, or a specific class or type of chemical reactions, it is envisioned that beneficial microreactors will incorporate the ability to facilitate a plurality of different processes related to the production of a desired product from a plurality of reagents. Generally microreactors will facilitate the mixing of a plurality of reagents. It should be noted however, that not all reactions require the mixing of reagents, such as reactions involving passing one or more reagents over a catalyst impregnated surface, or photochemical reactions that are initiated by the application of light of the appropriate wavelength. Preferable microreactors will enable the precise temperature control of the reagents and the product, so that yield and product quality can be enhanced. Other process control parameters that can be beneficially incorporated into microreactors for use in the present invention include magnetic, piezoresistive, piezoelectric, shape memory, radioactive, catalytic, optical, electromagnetic, and electrostatic control parameters. Any such control parameter is preferably capable of being controlled by control module 12. Thus in system in which the microreactor within reaction module 18 is capable of performing a plurality of processes, the selection of a specific desired chemical product by a user navigating through optional reaction database 26 will determine which of the plurality of processes supported by the microreactor will be utilized by control module 12 to produce the desired product. In systems not including optional reaction database 26, the user will manually enter known control parameters for the reaction (via user interface 28), enabling control module 12 to selectively control the required processes to achieve the desired product.
Reaction module 18 preferably includes a plurality of temperature sensors 54. These temperature sensors are electrically connected to control module 12 via power/data bus 48 in both reaction module 18 and pump module 14 and via conductors 49. Control module 12 uses data derived from the signals produced by the plurality of temperature sensors to adjust the flow rates of the heat transfer fluid (using pump 42 of pump module 14) to maintain the desired temperature parameters within microreactor 52. It should be noted that either more or fewer temperature sensors can be beneficially employed within the reaction module than the three illustrated in
Product exiting reaction module 18 via product fluid line 36 e enters residence time module 20 a and is directed into a capillary passage 56. Capillary passage 56 is wound around an inner cylindrical core 60, which is covered by an outer shell 58, thereby forming a heat exchanger. Heat transfer media from reaction module 18 and fluid line 36 c flows within the region defined by the inner core and outer shell, thus bathing capillary passage 56 in a flow of heat transfer fluid. In a preferred embodiment, capillary passage 56 is of sufficient length to achieve a 45-minute residence time at a flow rate of one milliliter per minute. Generally, a residence time of 45 minutes is sufficient for the majority of most chemical reactions to reach completion. If it is known that a particular chemical reaction can benefit from an increased residence time, an additional residence time module can be added downstream of residence time module 20 a, or a longer capillary passage can be used in place of capillary passage 56.
The product exits capillary passage 56 via fluid line 36 e and flows to a proportional valve 62. Several possible reactions can be performed in the system that are pressure dependent. These reactions include, for example, those involving decreasing volumes, increasing boiling points, and increasing gas concentrations in a liquid phase. Thus, specific positive effects can be achieved by causing a reaction to occur at a predefined pressure. To increase the pressure in the reaction path requires a throttle at the distal end of the reaction path. Closing the throttle makes the pumps in the pump module generate a higher pressure in the reaction module in order to maintain a constant flow rate. In this embodiment, the throttle comprises a proportional valve 62. Proportional valve 62 is electrically connected to, and thus operatively controlled by, control module 12.
It should be noted that with respect to the outlet side of reaction module 18, and both the inlet and outlet sides of any additional process modules 20 (or 20 a), that two reactant/product fluid ports 68 are not required, as only product passes through those sides of the modules. However, both reactant/product fluid ports 68 are included to maintain consistency relative to the configuration of these ports in all modules. With respect to pump module 14, both reactant fluid ports 68 are required so that Reactant 1 and Reactant 2 can be pumped from the pump module to the reaction module. On the inlet input side of reaction module 18, two reactant/product fluid ports 68 are required so that Reactant 1 and Reactant 2 can be directed to microreactor 52. Because Reactant 1 and Reactant 2 are mixed within microreactor 52, only a single one of the two reactant/product fluid ports 68 on the outlet side of reaction module 18 is used. In any additional processing modules 20, only the product, and not Reactants 1 and 2, flow through these modules, thus only one of the two reactant/product fluid ports 68 is used. It is envisioned that quick connecting bayonet type female/male connectors will be used to make the fluid connections between the fluid ports of adjacent modules. A bayonet connection 72 that encompasses the fluid ports and the power/data ports is also provided to maintain the individual fluid and power/data ports coupled and to provide a further fluid tight enclosure. Bayonet connection 72 is locked to the corresponding bayonet connection of an adjacent module by actuating a bayonet actuating lever 74. The bayonet actuating lever is included on each side of the housing to lock the bayonet connections together when the respective ports on adjacent sides of the modules are coupled together.
It should be noted that certain reactions may require further heat transfer media fluid ports or further reactant fluid ports to be provided on the modules. Those of ordinary skill in the art will readily understand that the required number of ports can be provided in the same locations on the housing of the modules so that all of the fluid connections are grouped in a single area and are consistently located and readily identified.
As indicated in
Reactant 1 fluid line 36 a and Reactant 2 fluid line 36 b enter the reaction module and are directed to microreactor 52. The reactant fluids flowing through these two fluid paths are mixed within the microreactor and a reaction takes place, producing the desired chemical product. That product exits microreactor 52 through a product fluid line 36 e. It should be understood that the fluid paths for heat transfer media, reactants and the product through microreactor 52, are quite simplified as illustrated in
Product from reaction module 18 is directed to capillary passage 56. The length of capillary passage 56 is preferably selected to provide a desired residence time. As noted above, the length of capillary passage 56 in the exemplary preferred embodiment enables a residence time of approximately 45 minutes, which is generally sufficient time for a product to be thoroughly reacted before being transferred to collection vessel 22. Heat transfer media enters residence time module 20 a from one of heat transfer fluid ports 66 and flows through fluid line 36 c into the region between inner cylindrical core 60 and outer shell 58. The physical arrangement of the inner cylindrical core, the outer shell, and capillary passage 56 provides a heat exchanger, which maintains the product at the desired temperature. The heat transfer media exits the region between the inner cylindrical core and the outer shell via fluid line 36 c, which leads to one of the heat transfer fluid ports 66 at the opposite end of module 20 a. From there, the heat transfer fluid is directed either to an additional processing module, or to a flow reverser (generally a U-shaped tube) if the heat transfer fluid is to be returned to upstream modules. Spent heat transfer (from the flow reverser or additional process modules), enters residence time module 20 a via heat transfer fluid port 66 (i.e., the one that is not used by heat transfer media exiting the module) and moves through the module via fluid line 36 d. Note that fluid line 36 d is not involved in the moderation of temperature within residence time module, and merely enables spent heat transfer fluid to move upstream of the system to preceding modules, and eventually be deposited in spent heat transfer recovery vessel 16 f. Arrows have been used in
As noted above, the flow of the heat transfer media fluid can be arranged in either a serial fluidic system or a parallel fluidic system.
Step 1: Preliminary Work
Prior to producing any product, a user must first select the desired product with the user interface of the control module. Furthermore, it is possible that more than one reaction is capable of producing the same product, so the user may also need to choose a preferred reaction. Optional reaction database 26 within control module 12 can be useful in selecting the desired product and method. Once the proper reaction conditions have been determined, the appropriate reactants, solvent and heat transfer media that are required must be provided.
Of course, the selection of the reactants is based upon the specific product that is desired. A solvent is selected based on its compatibility with the reagents that will be used. The solvent will be used to flush the system. The selection of the heat transfer media is determined based upon the required reaction temperature. A heat transfer media that is useful at one reaction temperature may not be useful at a significantly different reaction temperature.
Specific pump modules, reaction modules and/or additional processing modules may be required, as a function of the desired product. Because the system of the present invention is designed to facilitate the interchangeability of modules, the user must ensure that the appropriate modules are provided for a desired reaction. The pump module used will depend upon required flow rates of the reactants and heat transfer fluid, while reaction modules used will typically depend upon reactor throughput and/or the specific design of the reactor required to implement a particular reaction. Finally, many products may necessitate the use of a residence time chamber, while others will not. The desired amount of product required is also a parameter that will effect the configuration of the system, as system capacity can be modified by increasing the flow rate provided by the pump module, and by using a reactor that can accommodate that flow rate. As noted above, if the reactants are pressurized gases, a separate pump module may not be required.
Once the modules have been properly selected to achieve the desired reaction, fluidic and electrical connections between the modules are made. Sources of the reactants, the solvent, and the heat transfer media need to be connected to the pump module. Empty vessels must be supplied to receive the product and the spent heat transfer media, and placed in fluid communication with the system.
Step 2: Select "Start"
Once the system has been properly assembled and the fluid connections have been made, the user initiates the production process by executing a "Start" command with the user interface of the control module. The control module user interface also includes a "Stop" command that can be used to stop production at any time. Once started, and until stopped or a preprogrammed product volume is delivered, the control module will automatically operate the system.
Step 3: Thermal Conditioning of the System
Once the Start command has been received, the control module will begin pumping heat transfer media into the heat exchangers of the system. Heat exchangers will typically be included in the reaction module, and can also be included in any additional process modules. Preferably, the system will include sufficient temperature sensors so that the control module can determine when the desired thermal conditions have been achieved, and so that no reactants are input to the system until that time. Thermal equilibrium is considered to have been obtained in this embodiment, when the temperature sensor data indicate no more than a 2 degrees Kelvin difference separates the system temperature from the desired temperature. Alternatively, the control module can be programmed to wait a predefined amount of time before introducing reactants into the system after the start command was actuated to enable the heat transfer media to bring the system to the desired temperatures.
At the same time that thermal conditioning is occurring, the control module will use the solvent to flush the reactant fluid passages and lines of the system. Particularly when a residence time module is included within the system, the flow rate for the solvent flush may be increased significantly over the flow rate employed for the reactants, to reduce the time required for the flushing step.
Step 4: Synthesis
Once the system has reached thermal equilibrium, the solvent flush is terminated by closing the appropriate valves and the reactants are pumped to the reaction module at the proper flow rates. Reactors designed to perform different operations can be installed in the reaction module. Reactor operations typically will include thermally preconditioning the reactants prior to mixing them, and precise temperature control of the mixing area and the product produced by the reaction. In addition, reactor operations may include the use of a catalyst, or the application of various types of energy or radiation as described above. The product of the reaction then exits the reactor and moves to either an additional processing module or a collection vessel. In most reactions, any additional module employed will be a residence time module, although if the reaction requires multiple reaction steps, the additional processing module will then likely include another reaction module.
If a residence time module has been included, the product enters the residence time module where the product resides for a period of time that has been determined to be sufficient to complete the conversion of the reactants into the product. One or more heat exchangers are typically used to maintain thermal equilibrium of the product in the residence time module.
Step 5: Cleaning Cycle
Once the desired volume of product is produced (which may take a considerable length of time, as the system is designed to enable continuous synthesis of a product), the system is once again flushed with solvent. This flush can be performed manually or under the direction of the control module. If the system is continually performing the same reaction for an extended period of time, it may be beneficial to interrupt the production of product and perform a system flush as a maintenance procedure at regularly scheduled intervals.
As noted above, particularly preferred embodiments of the present invention will implement a stacked plate microreactor. The following disclosure, originally provided in the commonly assigned co-pending parent application (U.S. patent application, U.S. Ser. No. 09/496,999, entitled "MINIATURIZED REACTION APPARATUS," which was filed Feb. 3, 2000), describes a reactor for reacting one chemical with at least one other chemical, for the purpose of forming a chemical product. The reactor includes a plurality of simple plates, each simple plate having at least one opening formed therein, the simple plates being stacked together to form a plurality of layers and arranges so that at least one opening in each simple plate overlaps at least one other opening in an adjacent simple plate, thereby forming at least one pathway between at least some of the layers.
Unlike prior art stacked layer chemical reactors that require relatively complicated surface features, such as grooves or channels that do not penetrate the component to be formed into each layer, the simple plates employed in the present invention require no more than an opening be formed through each plate. Machining or stamping openings into a flat plate is significantly less complicated than the silicon etching, injection molding, and ceramic molding/sintering processes described in the prior art for producing the surface features that the prior art uses to channel fluid flow. Yet the relatively simple technique of forming openings in a flat plate can be used to achieve a very useful chemical reactor, if the openings are properly placed, and the plates are properly configured and stacked so that the openings in the plates cooperate to convey fluids through the apparatus.
In the following description and the claims that follow, it will be understood that the term "simple plate" means a plate that has substantially planar opposed surfaces, e.g., a flat sheet of material. In an exemplary reactor, no openings penetrate the peripheral edges defining the perimeter of the simple plates, and fluid passages used to implement heat exchangers are not in fluid communication with fluid passages for reactants or products, or fluid passages corresponding to reaction volumes and mixing volumes. The simple plates used in the embodiments of the present invention disclosed herein are all generally rectangular and are characterized by having one or more openings that pass completely through the simple plate. Thus, the term "simple plate" as used herein and in the claims should be understood to mean a plate that does not include any etchings, grooves, or channels that do not completely penetrate the plate.
The term "groove," as used herein, should be understood to mean a surface feature that has been formed into the surface of an object that does not penetrate completely through the object, and applies to components of prior art chemical reactors.
The plurality of stacked simple plates enables a reactor to be constructed that performs from one to all of the following functions: reactant conditioning, control of reactant supply, thermal pre-treatment, combination and mixing of reactants under controlled thermal conditions, intermediate thermal treatment, post-procedural isothermal containment, post-procedural thermal treatment of reactant products, and product separation. In particular, simple plates can readily be designed and fabricated in which the dimensional characteristics of the reactant fluid passages formed by the interconnected openings of the simple plates provide for a stacked laminar flow of the reactants. Such a stacked laminar flow ensures that a particularly efficient type of mixing, referred to as diffusion mixing, can occur.
The fluidic system of the stacked simple plate reactor is preferably characterized by having a small pressure drop across the entire system. Furthermore, potential clogging problems are minimized by having few constrictions within the reactor, by introducing as few sharp directional flow changes as possible, by maintaining a small inner volume (about 1 ml), and by enabling rapid diffusion mixing in the mixing portion of the reactor. Preferably, fluidic channel geometries range from 100–500 μm, especially with respect to reactant fluid pathways (the dimensions of any heat transfer media pathways are less critical), and the walls separating the heat transfer media from the reactants or product should be of similar scale, to enable rapid heat transfer. As discussed above, several materials can be used to fabricate a stacked simple plate reactor; however, simple plates that are adjacent to openings in those simple plates comprising heat exchangers are preferably fabricated from a material that has good thermal conductivity. However, if the dimensional thickness of each plate adjacent to a heat exchanger is small, on the order of 0.3 mm, the effect of the thermal conductivity of different materials is negligible.
In general, the openings in each simple plate of a stacked simple plate reactor correspond to a fluid pathway established by stacking a plurality of simple plates, such that openings in simple plates above and below overlap, thereby allowing fluids to move throughout the reactor. Openings may also correspond to passageways for sensors, particularly temperature sensors. Preferably, to maximize heat transfer, the fluid flow directions of the heat transfer media within openings defining a heat exchanger are opposite to the direction of reactant flow.
Top simple plate 110:
3.0 mm.
Second simple plate 120:
0.3 mm.
Third simple plate 130:
0.3 mm.
Fourth simple plate 140:
0.3 mm.
Fifth simple plate 150:
0.3 mm.
Sixth simple plate 160:
0.3 mm
Seventh simple plate 170:
0.2 mm.
Eighth simple plate 180:
0.3 mm.
Ninth simple plate 190:
0.6 mm
Tenth simple plate 200:
0.3 mm.
Eleventh simple plate 210:
0.2 mm.
Twelfth simple plate 220:
0.3 mm
Thirteenth simple plate 230:
0.6 mm.
Fourteenth simple plate 240:
0.3 mm.
Fifteenth simple plate 250:
0.3 mm
Sixteenth simple plate 260:
3.0 mm
Simple plates 110 and 260 (the top and bottom simple plates) are thicker than other plates to provide greater structural stability. Simple plates 120–160, 200, 220, 240 and 250 are much thinner, to enhance heat transfer. As will be discussed below, a thickness of 0.3 mm provides a reasonable heat transfer ability for a wide variety of materials.
For simple plates that include solid portions used to transfer thermal energy to or from heat exchangers, a preferred thickness is about 0.3 mm. As plate thickness increases, mechanical stability increases and heat transfer ability decreases. The 0.3 mm thickness provides good heat transfer characteristics without sacrificing mechanical stability. When graphs representing mechanical stability as a function of plate thickness (50 μm–1 mm) and heat transfer ability as a function of plate thickness (50 μm–1 mm) are combined, the curves representing each functional relationship intersect at approximately 0.3 mm. It should be noted that this optimum value of 0.3 mm is independent of the actual material selected (glass, metal, plastic, etc.). While the shape of the curves defining the functional relationships change when a different material is selected, the intersection of the curves at 0.3 mm remains relatively constant. Thus, 0.3 mm represents a simple plate thickness that provides for reasonable heat transfer ability without sacrificing structural integrity.
In the fifth layer, fifth simple plate 150 incorporates a plurality of reactant A openings 155 that are aligned with a plurality of Reactant B openings 157 (see
In layer 8, the shape of heat transfer media A intake manifold 182 a changes once again. The purpose of the size change between the heat transfer media A intake manifolds in layers 7 and 8 is so that heat transfer media A can be fed into two separate sections of the layer 9. In a first heat transfer media A fluid path in layer 9, heat transfer media A flows into a heat transfer media A intake manifold 142 a, and from there to heat transfer media A intake manifold 42 a of tenth simple plate 200 in layer 10. From there, heat transfer media A flows to heat transfer media A intake manifold 142 a in layer 11, an enlarged heat transfer media A intake manifold in layer 12, and then to heat transfer media A intake manifold 142 a in layer 13.
In a second heat transfer media A fluid path in layer 9, fluid flows out of heat transfer media A intake manifold 182 a of eighth simple plate 180 and into third heat exchanger 193 on ninth simple plate 190 of layer 9. The purpose of third heat exchanger 193 is to moderate the temperature of the solid portion of layer 10 immediately adjacent to reaction channels 116 in layer 11. Heat transfer media A exits heat exchanger 193 by returning to layer 8 via heat transfer media A exhaust manifold 182 a, which is enlarged and overlaps the right end of third heat exchanger 193.
Simple plate 200 of layer 10 includes enlarged heat transfer media A intake manifold 182 a (as well as exhaust manifold 182 b). It should be noted that reaction channels 116 of layer 11 are not quite long enough to overlap the enlarged heat transfer medial intake and exhaust manifolds 182 a and 182 b, thus no heat transfer media enters reaction channels 116. Here, the functional purpose of the size change of the intake and exhaust manifolds is to reduce the surface area of tenth simple plate 200, to enhance bonding, rather than to feed a heat exchanger (as in layer 8 and eighth simple plate 180).
Referring now to layer 11, note that again the size and shape of heat transfer media A intake manifold 142 a has changed relative to the intake manifolds of layers 8 and 10. This size change relates to maintaining a calculated fluidic equilibrium throughout the micro reactor. However, it is contemplated that the overall effect of the size change is relatively minor, and that an effective micro reactor can be achieved without changing the size of the intake manifolds on layer 11.
In layer 12, the size and shape of heat transfer media A intake manifold 182 a is again enlarged, to once again divert some heat transfer fluid A into a second fluid path that services fourth heat exchangers 133 a and 133 b of layer 13. Heat transfer media A also flows into a heat transfer media A intake manifold 42 a in layer 13. The functional purpose of heat transfer media A intake manifold 142 a of layer 13 is to ensure that the fluid pressure within fourth heat exchangers 133 a and 133 b matches the fluid pressure within third heat exchanger 193. Note both the third and fourth heat exchangers are moderating the temperature of reaction channels 116, and thus preferably both heat exchanges should have similar flow characteristics.
Heat transfer fluid A that has entered fourth heat exchangers 133 a and 133 b exits layer 13 via heat transfer media A exhaust manifold 142 b in layer 12. From there, heat transfer media A moves successively through heat transfer media exhaust manifolds 142 b in layer 11, 182 b in layer 10, 142 b in layer 9, 182 b in layer 8, 142 b in layers 7–4 and 122 b in layers 3–2. Heat transfer media A finally exits the reactor via outlet 112 b in top simple plate 110.
Generally the heat transfer media used in the preferred reactor will be liquids, although it is envisioned that selected gases may also be beneficially employed. Fluidized solid heat transfer media (such as sand or silica) are known in the art, and might be used, though the dimensions involved in the fluid channels of the preferred reactor raise the concern that the solid heat transfer media could cause clogging of the heat transfer pathways.
Although the present invention has been described in connection with the preferred form of practicing it and various modifications thereto, those of ordinary skill in the art will understand that many other modifications can be made to the present invention within the scope of the claims that follow. Accordingly, it is not intended that the scope of the invention in any way be limited by the above description, but instead be determined entirely by reference to the claims that follow.
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|International Classification
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|Apr 6, 2001
Owner name: CELLULAR PROCESS CHEMISTRY, INC., WASHINGTON
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SCHWALBE, THOMAS;OBERBECK, SEBASTIAN;GOLBIG, KLAUS;AND OTHERS;REEL/FRAME:011688/0344
Effective date: 20001025
|Apr 23, 2008
Owner name: YMC CO. LTD., JAPAN
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:CELLULAR PROCESS CHEMISTRY, INC.;REEL/FRAME:020837/0877
Effective date: 20080414
|Jan 11, 2010
|Maintenance fee reminder mailed
|Jun 6, 2010
|Lapse for failure to pay maintenance fees
|Jul 27, 2010
|Expired due to failure to pay maintenance fee
Effective date: 20100606


text:
20 Best Self Improvement Books
Being perfect means to be emotional and physically better than what you were yesterday. It is true that no one is just perfect. A lot of hard work and improving needs to be done in order to reach a stage at which one can feel that they have become what they aimed to be, a… Read More »

subset: commoncrawl


text:
CC: Jeb Bush, Ted Cruz, Rick Perry, Scott Walker, Marco Rubio, Chris Christie and Carly Fiorina
Quad City Times // Editorial Board
Just last week, Indiana Gov. Mike Pence invited a handful of religious conservatives to a private signing of his Religious Freedoms bill, a vague appeal to religious exclusionists aligned with anti-gay initiatives. The bill flew through Indiana's Republican-controlled legislature. Just five Republicans voted against it. …So the Indiana governor's socially conservative tactic didn't just backfire. It ignited a war between Indiana's traditional conservatives and the tea party wing Pence helped bring to power.
Indiana needs to clarify or drop discriminatory law
Dubuque Telegraph Herald // Editorial Board
That Indiana is facing a firestorm of criticism and protest over last week's enactment of a so-called Religious Freedom Restoration Act may not say as much about the Hoosier state as Americans' shifting attitudes over gay marriage and LGBT issues…There has been significant movement over the past few years regarding Americans` attitudes toward gay marriage and other LGBT issues. The pendulum has swiftly swung away from discrimination. Owners of businesses have no better reason for refusing to sell a gay couple flowers or a cake for their wedding than their ancestors did for refusing to serve blacks at lunch counters and hotels 50 (or fewer) years ago. Providing a product or service to a LGBT customer is not an endorsement of the customer`s lifestyle. The customer wants to buy flowers or photographs, not drag the business owner to church or a gay-pride parade.
New Indiana law is a step backward for civil rights
Iowa State Daily // Editorial
Indiana took a big step backward in civil rights on Thursday when Gov. Mike Pence signed the Religious Freedom Restoration Act into law. The new law will allow Indiana businesses to legally refuse services to people who are gay. This is the first bill to become law under a movement of states that have legislation moving through the state legislatures to "protect religious freedoms."…Those who worry that the vague nature of the law's language will create a gray area that facilitates discrimination have more than enough reason for concern, especially because the law itself is a nearly textbook example or dictionary definition of discrimination.
New Hampshire
Indiana makes N.H. look progressive
Nashua Telegraph // Editorial
The uproar in Indiana will probably put an end to talk about Mike Pence as a possible presidential candidate – he made a test-the-waters visit to New Hampshire in the fall – but more importantly, it should serve as a lesson to those who favor greater religious protections. The way to achieve it is not by discriminating against others. Anyone with even a passing familiarity with religious history should know that.
Discrimination bill is indefensible
Monadnock Ledger-Transcript // Editorial
Big businesses have already threatened to pull their money and events out of the Hoosier state. Several states, including New York and Connecticut, have banned state-funded travel to Indiana in the wake of the bill's signing. But there are a vocal few who have made their support of Gov. Pence and the bill quite clear: the majority of the perceived frontrunners for the 2016 Republican presidential nomination. Former Florida governor Jeb Bush fired up the bandwagon, and was quickly joined on his ride by Senator Ted Cruz of Texas and Senator Marco Rubio of Florida, all of whom defended Gov. Pence in lockstep.…These politicians need to be held accountable for their stance on this issue, and when voters and media members have their chance to question the potential nominees, we hope they won't have forgotten this misstep. Discrimination under any guise is just plain wrong, and it's hard to imagine electing someone for any position who feels otherwise.


text:
Thomas Sankara's Vision: Panafricanism, Internationalism, and Socialism
By Heather Benno
This text is from a presentation by Heather Benno, Lawyer, Human Rights Activist, and Member of Answer Coalition during the Second Edition of the Thomas Sankara Annual Conference held in Washington, DC on October 12, 2013.
In his Political Orientation Speech of October 2, 1983, Sankara laid out the National Council of the Revolution's (CNR) program for the revolutionary rebirth of the nation [Upper Volta]. These core goals of the revolution reflected the need for the revolution to make alliances with other revolutionary struggles and anti-imperialist struggles around the world: both to advance those struggles, and to protect and advance the revolution at home. It established a framework by which the revolution would conduct international relations – not on the basis of expansion, enslavement, profiteering or military power as has been the practice of the United States and the European powers – but on the basis of mutual development, national liberation, and political support.
In his Political Orientation Speech of October 2, 1983, Sankara laid out the National Council of the Revolution's (CNR) program for the revolutionary rebirth of the nation [Upper Volta]. These core goals of the revolution reflected the need for the revolution to make alliances with other revolutionary struggles and anti-imperialist struggles around the world: both to advance those struggles, and to protect and advance the revolution at home. It established a framework by which the revolution would conduct international relations – not on the basis of expansion, enslavement, profiteering or military power as has been the practice of the United States and the European powers – but on the basis of mutual development, national liberation, and political support.
"We must define the place of the … revolution in the world revolutionary process. Our revolution is an integral part of the world movement for peace and democracy against imperialism and all forms of hegemonism. That is why we will strive to establish diplomatic relations with other countries on the basis of the following principles:
(1) Respect for each other's independence, territorial integrity and national sovereignty;
(2) Mutual nonaggression;
(3) Noninterference in domestic affairs;
(4) Trade with all countries on equal footing and on the basis of mutual benefit.
And Sankara boldly declared solidarity with the national liberation and anti-imperialist/anti-racist struggles on the continent and those farther away.
"We will give active solidarity and support to national liberation movements fighting for the independence of their countries and the liberation of their peoples. This support is directed in particular:
(1) To the Namibian people, under the leadership of the SWAPO
(2) To the Saharawi people, in their struggle to recover their national territory;
(3) To the Palestinian people, for their national rights.
Objectively, the anti-imperialist African countries are allies in our struggle. The neocolonial alliances operating on our continent make closer ties with these countries necessary."
Sankara's concept of strength through unity and development by building anti-imperialist alliances led him to travel frequently throughout Africa and around the world, forging alliances with other nationalist and anti-imperialist leaders that were willing to lend political and at times economic support to the Burkinabe revolution without any exploitative terms.
This cross-border Panafrican unity would strengthen nations in the face of the ploys of the West to divide nations with war and exploit all of their resources. He explained, in references to Burkina Faso's relations with Ghana, "The spirit of liberty and dignity, of counting on one's own resources, of independence, and of consistent anti-imperialist struggle should blow from north to south and from south to north, crossing borders with ease."
Sankara drew from the history of the U.S. and Europe in Africa, including the Middle East, and Asia. Just 28 years prior, President Gamal Nasser nationalized the Suez Canal in July 1956 in an act of defiance to world imperialism. Algeria won its independence in 1962. There had been an inspiring escalation in national liberation and independence struggles on the continent and around the world. Libya under Qaddafi was an ally.
Yet as of August 1984 – one year after the revolution, Sankara was still forced by world circumstances to pose the question: "Do you think our country would have any problems or difficulties in its relations if that wind were blowing through our country and all the other countries? Do you think countries would have gotten to the point of threatening each other with the apocalypse today if this same wind were blowing through all the countries of the world? Currently we're talking about Iran and Iraq – [in reference to the Iran/Iraq war] – don't you think it would be good if Iranians could go visit Iraqis in the same way that Ghanians go visit Burknabe and vice versa?" The imperialist fueled Iran/Iraq war lasted 8 years and resulted in hundreds of thousands of deaths.
To the United Nations, two months later, Sankara elaborated by voicing support for numerous struggles, including the anti-apartheid struggle in South Africa, Angola and Namibia, the "valiant Palestinian people," and with the soldiers "of Iran and Iraq who are dying in a fratricidal and suicidal war." He also expressed solidarity with the struggle in Nicaragua and all across Latin America, in Afghanistan and Ireland, and the peoples of Grenada and East Timor.
He demanded progress in the Burkinabe, continental and international struggle for women's liberation, which he noted could not be separated from political struggle for self-determination and independence.
In defending the new Burkinabe revolution, Sankara took on the role as the "spokesman for all those who vainly seek a forum in this world where they can make themselves heard." So we tonight speak in his honor on "behalf of all 'those left behind - '" including those still fighting and clinging to the struggle for independence and self determination today.
Today, the people of the Middle East, the African continent, Asia, Latin America – and indeed the working people of the United States - have no smaller of a feat. Yet we in the United States have not yet made a revolution that could redirect the vast resources of this country from military death and destruction to revolutionary support and solidarity assistance. When there was a revolution in Tunisia, kicking out a U.S.-backed dictatorship that robbed the people, the people of the United States wanted to stand in solidarity with that revolution, but the U.S. government – bought and sold by multinational corporations that do not serve our interests – was intent to reining in any renewal of revolutionary fervor in the Middle East and on the African continent.
The Obama administration has increased the drone war on Africa, continued a campaign of murderous bombing in Somalia, enraging the people of the region again imperialism anew. It is also increasing its military presence and aggression in Mali, Niger, and across the continent of Africa, and continuing US interventions in the people struggles in Egypt and around the world.
We saw a truly anti-imperialist struggle break out in the United States in response to the war on Libya, the murderous bombing of Libya, and the murder of the former leader of that country Colonel Gaddafi, and also in response to a threat of another war on Syria.
Thankfully the world Goliath, the world imperialist today, the United States of America, was forced to put that imperialist aggression on the break.
In closing I leave you with the following words of Thomas Sankara he pronounced in Harlem in 1984: "I am not going to speak long because those who spoke before me said about a revolution should be. What is left for us to do is to make the revolution."
Thank you! .
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Category Archives: Pakistani Politics
Partition: the 67-year itch ~ (by Irfan Husain)
The following is a guest post by Mr. Irfan Husain. The article was originally published in the journal of the Pakistan Institute of International Relations. Like an itch that won't go away, people of my generation born before Partition keep scratching away at the words, actions and motives of the players involved in that momentous event. Each time we traverse this ... Read More »
Words That Kill
The following is a guest post by Mr. Irfan Husain. The article was originally submitted to Dawn by Mr. Husain, who is one of their regular op-ed writers. However, due to its contents, Dawn found itself unable to print it. I don't know if there are official rankings for the sleaziestTV personality in Pakistan, but if there were, Amir Liaquat ... Read More »
Some thoughts on the horrific Peshawar attack
1. In the overall context of the state's war against the Taliban and its affiliates, this has been probably the best year since 2007. Fewer civilians are dying in Pakistan in terrorist attacks today than in the last half decade (data source: SATP). The above graph probably understates the level of drop-off, since it includes deaths from all over Pakistan, ... Read More »
The Sharif Family
As promised at the end of the previous post, here's some extended detail into the wealth of the Sharif family. Almost all comes from publicly available documents that the politically active members of the family have filed at the time of contesting elections, or regular asset declarations as members of legislature, as required by the law. Starting with some history. The Ittefaq ... Read More »
Fake 'Richest Pakistani' lists
Well, this post is just because I'm fed up of telling sane minded, non-mentally challenged people again and again that there are no 'official' lists of wealthiest Pakistanis, or one prepared by a reputable financial outlet (ala Forbes' listings). Still, the kind of idiocy that goes around has no limits. Since fake fortune lists are ever more viral and are now annually ... Read More »
Fingerprint Verification – Part 3
This is the third in a series of posts on the 'fingeprint verification' of ballots in Pakistan. I first wrote about it in September 2013, when the whole exercise was picking up steam as some forensic way of settling electoral fraud debates. The second part was in July 2014, and expanded on the misrepresentation of facts from the NADRA reports ... Read More »
Fingerprint Verification
I have written about it before. Earlier. It was on how the majority of votes cannot even be verified. You can check that out here, and please read it before reading this post. Let's start with hearings of complaints at Election Tribunals. Firstly, they are beyond the purview of the executive. Imran keeps on demanding the government or the challenged ... Read More »
Some questions about the North Waziristan operation
I do not know the answers to these questions: 1. Which groups are being targeted? 2. Which groups are not being targeted? What does it say that the likes of JuD have explicitly come out in support of the operation? 3. What are the strategic goals, if any, meant to be accomplished by this operation? Is this employment of force ... Read More »
Thinking out loud about what a "Taliban victory" in Pakistan looks like
I'm using this post mostly to think out loud about something I have been thinking about for a few months, so please bear with me if some of it is dumb. Mostly I'm trying to think through the tension between two narratives that seem reflexively acceptable: The TTP is a loose coalition of fighters with varying degrees of attachment to ... Read More »


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These are a list of the websites that support the coupling of Dr. Gregory House and Dr. Lisa Cuddy. If you know of any, please post them below.
The Huddy Realm : A fanfiction archive, dedicated exclusively to House/Cuddy fic. You can register and then post and manage your own Huddy fics.
Blogcritic : A two-part article summarizing the development of House and Cuddy's relationship from seasons 1-6.
Buddy TV : The top ten Huddy moments.
Discussing the breakup - David Shore on Season 7
See also Huddy
|Notice: This article is a stub, please help House Wikia by expanding it.


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Greene, an all-state first team selection by the Associated Press, consistently practiced hard, and showed his ability to get through the line of scrimmage quickly.
While some coaches expressed frustration at how a few players were practicing, that wasn't the case concerning the uncommitted Greene, who is considering North Carolina State and Rutgers ahead of Alabama and Auburn.
"Our running backs coach (Bobby Saunders) tells us to finish each play,'' the 6-foot, 200-pound Greene said. "It's natural. The coach back at (Irmo) taught me that, too. Coach is enforcing that I finish every play and have the ball in the correct hand, speed through the hole, reading my linemen.
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Despite being hampered by an ankle injury and being limited to six games, Greene rushed for 1,367 yards and 13 touchdowns in six games.
The upgrade in competition in this week's practice has allowed Greene to gauge his playing ability, and the results are looking good.
"I'm getting a lot better,'' Greene said. "The linebackers are supposed to be playing in college, so I have to beat them to the edge, beat them to the hole.''


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According to Mayo Clinic, strep throat is contagious. The bacteria that cause strep throat are known as streptococcal bacteria. Strep throat may be spread through coming into contact with airborne droplets from an infected person's choking or sneezing or through sharing beverages or food with that person.Continue Reading
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Is Mila Kunis Wearing An Engagement Ring?
Have you ever seen her look like that? No.
She has the serious face of a pregnant woman who just realized her life is about to change big time.
Next year Mila will be having a baby, and Scarlett will be having one too. So will Gwen Stefani. 2014 babies.