MXPA02005183A

MXPA02005183A - Continuous coking refinery methods and apparatus.

Info

Publication number: MXPA02005183A
Application number: MXPA02005183A
Authority: MX
Inventors: E Brecher Lee
Original assignee: Univ Wyoming Res Corp D B A We
Priority date: 1999-11-24
Filing date: 2000-11-21
Publication date: 2002-11-07
Also published as: CA2393120A1; BR0015733A; AU1787701A; EP1246888A1; CA2393120C; EP1246888A4; WO2001038458A1

Abstract

A system for refining hydrocarbon containing materials in a continuous coking mode may provide a pyrolyzer (1) which may be inclined to effect a liquid seal between a liquid conduction environment (6) and a gaseous conduction environment (7). A heat source (9) may heat the material past the coking point and the system may include a screw or auger (10) which can continuously remove the coke while simultaneously outputting refined products.

Description

METHODS AND REFINERY APPARATUS WITH CONTINUOUS COKE FORMATION I. TECHNICAL FIELD The present invention relates to apparatus methods for refining heavy oils, such as in the transformation of heavy oils into lighter, or higher quality components, which are more commercially useful.

II. PREVIOUS TECHNIQUE Everyone is aware of the importance that oil and other such materials have today. They represent an important topic from a large number of perspectives, from environmental to economic and to politics. At a chemical level, these materials are significant, because the substances of which they are composed have hydrogen and carbon with molecules whose structures easily supply energy when they are burned. In some cases, the raw materials, which occur naturally are already at your convenience. For example methane, CH4, a "natural gas" - as its name implies - is often available in a preferred chemical composition in nature. However, some hydrocarbons do not occur significantly in a preferred state in nature. Fortunately, many of the hydrocarbon molecules can be easily separated or transformed through thermal and chemical processes. The transformation separation, usually made on a large scale, with the creation and collection of the desired species, is a process popularly known as a "refining" of material. For most people, what a refinery does is take the raw material, which occurs naturally, and refine it in one or more ways, which are more convenient commercially. As an example, the heavier molecules found in the bitumen can be divided into lighter components through the processes of refining. From a simplified perspective, the process of refining the material involves heating and altering the composition of the combustible materials by distillation, rupture or decomposition of the larger and smaller molecules, expelling the various species with volatile components, and then collecting the substances in the desired form. Many refinery processes produce coke. When hydrocarbons are heated above certain temperatures, they can reach a point at which carbon atoms join together and form a substance known as coke. This coke can be problematic because it is a very hard and relatively transformable substance, which usually binds to its contents when it is formed. Great difficulties are present in the processes related to coke. For example, there is a technique, recently invented, to identify the point at which coke can be formed precipitously. This technique, described in PCT Application No. PCT / US00 / 15950 incorporated herein by reference, shows great hopes. Coking processes require careful handling. Here, processes are often achieved in a modality in lots or semi-batches. After the coke has formed, the container is set aside to remove, by pneumatic hammer or otherwise, the coke itself. By nature, a true continuous process is difficult to achieve. In addition, because many capital expenditures are required in such management, currently only large refineries now use coking as the main method of improving heavy crude oils. Thus, while it is convenient for efficiency, the smaller refineries do not * have been able to practically use coking processes on a commercially viable basis. Since the crude oil supplied by the refineries becomes heavier, this need may be more critical. However, despite this need, a solution to the precipitate formation of the coke and the availability of the coking processes has not been available in the desired commercial grade. Certainly, the importance of the refining process is well known. S has perceived the need, not satisfied, of greater efficiency, greater availability and better management of said processes. Despite feeling this need for some time, however, an appropriate process has not been available. As the present invention shows, through a different approach to the problems, there may be a solution. Perhaps, surprisingly, the present invention shows not only that a solution is available, but also shows that the solution is one that, from some perspectives, can be considered using existing techniques and elements of realization. Adapting some characteristics of other stress fields (such as the resource or the toxic waste recovery fields, as mentioned in U.S. Patent No. 5259945), the present invention can solve many of the problems already experienced. in the refinery fields. To an extent, the present invention can be considered as showing that in the refinery field, those skilled in the art may have been simply too limited to one perspective and while there have been substantial attempts to achieve the desired goals, they have failed, such due to lack of proper understanding of the problem of coke formation in the appropriate context. In fact, the efforts may even have deviated from the technical direction in which the present inventors go, and thus the results may be considered as unexpected. Thus, the present invention may not merely represent a major advance in the previous art, and may provide a critically different approach, which provides the ability to use the coking process, while also providing a continuous process operation. As will be seen, the physical characteristics that allow this critical difference in performance are not merely distinguished in the batch type process (as it could exist in a semi-batch mode), and are completely different from the present treatment of the coke. and the processes. Thus, up to the present invention, no process has provided the ability to allow a truly continuous process of coking, in the commercially practical ways, now available. lll. EXPOSITION OF THE INVENTION The present invention provides a continuous refining process, which allows the intentional formation of coke from the material being processed, while acting to separate and perhaps create a greater quantity of refined product. In one embodiment, the invention uses an inclined auger, with a medium, such as sand, in which the raw material is heated, beyond the coking point. The auger then continuously moves the coke out of the bed, so constant and continuous refining can occur. Therefore, it is one of the many goals of the present invention to provide a system through which continuous refining can occur, even while allowing coke to be formed. To achieve this goal, the invention provides refining in one system, but with multiple zones, so that the continuous process can be conducted efficiently. Naturally, additional objects of the invention are described through other areas of the claims specification.

IV. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic view of an inclined auger type refining apparatus. Figure 2 is a diagram of an output of an embodiment of the present invention in an application. Figure 3 is a diagram of a hydrotreating result in the pyrolyzer of certain higher fractions. Figure 4 is a schematic view of a tip of the general system. Figure 5 is a diagram of one type of process material. Figure 6 is a diagram of the production of an embodiment of the present invention. Figure 7 is an estimation of the process cost of the drilling muds, in one embodiment of the present invention.

V. THE BEST WAYS TO CARRY OUT THE INVENTION As can be seen from the drawings, the basic concepts of the present invention can be incorporated in many different ways. Figure 1 shows a schematic view of an inclined barrel type refining apparatus, according to the present invention. This can be considered one of the many key components to an improved refining system. As an important feature of a modality, the system is designed not only to be able to accept material containing heavy hydrocarbons, but can do so in a continuous manner. As shown in Figure 1, the refining apparatus may include a pyrolizer (1) having a container (5) of the process, within which refining may occur. This pyrolyzer (1) can have some kind of inlet (2), through which the material, which will be processed, can travel. To remain in one of the objects of the invention, the entry (1) can be continuous, so that the material is supplied within the pyrolyzer (1) the same regime with which it is processed. The material process can, of course, result in refined products that can flow out of an outlet, such as the outlet () for volatile materials. It can also result in a residue or unrefined material, or maybe it can not be refined. This can flow out through some type of outlet, such as the outlet (4) of the waste. As mentioned before, a desired aspect of at least one embodiment is the ability to process heavy hydrocarbon material. This is why it is not only the traditional definition of "heavy" tried, but also the specific goal, such as the ability to continually enter a material that has an API gravity of at the 11th API, heavy oils, asphalts, bitumen tars, material having an API gravity less than about 11 ° API, material having an AP gravity of less than about 10 ° API, material having an API gravity of less than about 7 ° API, and even material having an API gravity of less than about 3 API In addition, in one embodiment, there is also the desire to be able to handle and process materials that have significant amounts of waste, including, but not limited to, materials that have at least 5% by weight of waste materials that have at least 7% by weight of waste materials having at least 10% by weight of waste, even materials that have at least 15% by weight or more residue. The pyrolyzer (1) can alter the chemical composition of the material to be processed. This material can of course include a variety of crude oils, but also materials such as separation funds, and the like. For the most effective process, this can be achieved through thermal decomposition coking reactions, which re-arrange the hydrocarbon and redistribute the hydrogen. For example, through one embodiment of the present invention, applied to the Cold Lake crude product process, approximately 55% of the evaporated bottoms fed to the separator is recovered as a distillate, while 45% flows as a subflow to pyrolyzer (1). The displaced product of the pyrolyzer (1 can still be a light distillate, free of residue, with an API gravity in the range of 25 to 60 degrees.) In an important form, the pyrolyzer (1) can produce an oil of light hydrocarbons, which, once stabilized, it can contribute significantly to the value of the general product.Rololization can include the coking of thermal decomposition of petroleum or heavy material, to produce light additional oil, free of residue, ga fuel for process energy, and a solid similar to petroleum coke, for land filling With reference to Figure 2, in this example, it can be understood that approximately 44% by weight of the pyrolyzer charge (1) can emerge as liquid, around 12% can emerge as a combustible gas and around 44% can emerge as coke.The pyrolyzer (1) can also be used to process solids, particularly in the case of solids. gone loaded with hydrocarbons. In one design, the pyrolyzer (1) can coke approximately 75 bpd (barrels per day) of heavy oil or even separate bottoms at temperatures of about 538 ° C. The pyrolyzer (1) can also be combined with other process elements, such as separators and evaporators or the like. While the pyrolyzer alters the chemical composition, the evaporation and separation operations can be thermal separations with a variety of options. As you can easily understand, the pyrolyzed (1) It can achieve the refining of hydrocarbon material using a refining environment and even substances that volatilize continuously. The system can then use those substances as they are or to form refined products. For example, the desired non-condensable gases can be recovered and reused as process fuels can be burned. As the material progresses further into a hot zone, thermal decomposition and coking of the heavier hydrocarbons remaining may occur. In one modality, this may have occurred at or even past the point of coking, thus, a greater amount of recovery and refinement may be achieved. Significantly, a system combines a coking type of process with a continuous input and continuously entering the material to be processed, to allow increased outputs. Thus, the input (2) to or process container (5) can be adapted to continuously accept material. It is important to understand that the system can provide a differential process 20. This can occur through the use of more than one refining environment. Po this, it must be understood that different driving temperature, location, flow or other types of zones can be achieved. Referring to Figure 1, it can be understood how a preferred embodiment can have multiple refining environments in even a process container (5). In this mode, the multiple zones are achieved by tilting the container (5) of the process and supplying it in a smaller condition than the full one. As shown, there is a first refining environment, such as the environment (6) d driving of the liquid completely and a second refining environment, such as the gaseous conduction environment (7). These environments can establish different thermal environments among which the temperature, driving regime or other thermal differences may exist. This can occur over an effective process length (8), and a container, such as the container (5) of a process. As shown, after introducing the material through the inlet (2), refining or refining of material can be initiated in a first refining environment, shown here as the liquid conducting environment (6). It can then be pushed, or pulled, or otherwise traveled to the refinement of the continuous material in a second refining environment, shown here as a gaseous conduction environment (7). After the material is introduced through the inlet (2), it can be heated by some type of heat source (9). [This, of course, can include a wide variety of heat sources and so shows only schematically.] This raises the temperature of the material and, as the temperature rises, different volatile substances are expelled. They can be collected through the outlet (3) of said volatile substances, as mentioned above. Since the energy is used to eject the volatiles, as the material traveled through the length (8) of the container (5) of the process, it can continue heating. This can expel other volatile products and can cause the thermal decomposition of the heavier hydrocarbons and may eventually reach a point at which the coke is formed for that material, and say at the coke formation temperature. As shown by the dotted line in Figure 1, the liquid conduction environment (6) finally ends and there is then the gaseous conduction environment (7). Inclining the container (5) of the process, this can exist at a distance. Thus a third refining environment can be considered to exist, here, an ambient which makes transitions between pure liquid and gaseous states. Again, as the material travels through the pyrolyzer (1), it can be considered as being subject to a third refining environment, here, the region in which there is a combination of the first and second refining environments, that is, the environment partially liquid and partially gaseous. This can provide advantages in refining. As you can understand, the third refining environment can be considered as a third thermal environment or a transition refining environment. Through the inclined design shown, this transition environment can present a gradual transition environment, or even a linear transition environment, so that the amount of one environment (liquid) decreases linearly, while the amount of another environment (gaseous) increase linearly. In this region, of course, there is an ambient of combined, liquid and gaseous driving. The location of the quantity and changes in the various environments of the process can be equally remarkable. As can be understood from the drawings, at least about the lower third of the process length (8), about one third of the container (1) of the process, may contain the one or some of the first refining environment or environment (6) of liquid driving. This can also be increased or decreased to other lengths. Particularly, even at least about half of the process length (8) or about half of the process container (5) can be used for the environment (6) d liquid conduit. Thus, in one embodiment of the inclined pyrolysis (1), a lower third or even the lower half may be the area of the liquid or non-volatilized material. As mentioned before, the material that is processed can be pushed, pulled, or otherwise traveled inside the pyrolyzer (1). This can be achieved affirmatively. This movement of the material can be from a first refining environment to a second refining ambient. As shown, a screw or drill (10 can be a way to achieve this movement, among other purposes.) This screw or hole (10) can thus serve as a movement element, which operates through the environment (6) of liquid flow and inside the gaseous conduction ambient (7) In the arrangement shown, the lower third to a half of the inclined screw, can be filled with hot liquid, which subsequently forms coke, which is drilled upwards and Figure 4 is a schematic view of a general system, according to one embodiment of the invention, it can be understood, the output (3) of volatiles can be fed [with or without a treatment (11) after refining] in some kind of collector, such as a condenser (12) Regardless of how it was designed, the collector will usually act for the output of the desired refined product.Often, of course, this can be done separately, if However, for simplicity, it shows conceptually only as a single output (13) of refined product. These various products accompany the collection of refined products or perhaps the condensation of at least some of the refining process results. As considered in a preferred mode, they will be configured and operated to collect refined products that have an API gravity of at least 25 ° API, up to at least about 60 ° API, no more than about 3.7% content of sulfur, no more than about 3.1% sulfur content, or even that have the characteristics of a combustible gas., So the elements can be adapted to receive at least some of the volatilized substances created by the processes of refining and to collect at least some of the refined product. In order to facilitate the refining process, a sweeping gas can be used. This is shown in Figures 1 and 4, where the inlet (14) of the swept gas d is illustrated. As shown, it may be advantageous to establish the entrance (14) of the sweep gas located behind the point e which ends the liquid, an area of a liquid seal, as discussed below. Additionally, of course, the output of the scavenging gas, shown as coincident with the outlet (3) of volatile products, can be established behind the liquid seal, in order to facilitate the removal of refined volatile products. In the heating of the material to be processed, it may be highly desirable to intentionally heat that material beyond the coking temperature. Thus, coke will probably be formed. More than merely having some incidental formation of the coke, this type of embodiment of the invention can intentionally and affirmatively exceed the temperature of coke formation within the material. This, of course, will result in exactly the substance that has previously been considered undesirable in some systems and can cause the formation of a substantial amount of coke from at least some of the materials (for example the material that has not been volatilized). The high residue material can thus be used efficiently, which includes, but is not limited to, the material that will result in at least 1%, 2%, 5%, 10%, 20% or even, as mentioned, the 44% of the weight material of the coke material. A variety of temperatures can be used to result in the formation of a substantial amount of coke from at least some of the material. This may include temperatures at the source (9) Heat is operated as a heat source of coke formation, to cause the material to achieve at least a temperature of 343, 371, 399, 426, 482, 509, 538, 593 ° C and even 648 ° C and more. As mentioned before, at least some of the material to be processed can be moved from the entrance to the exit. When coke is formed, this element can take on an additional role. The movement element, shown in Figure 1 as the screw or bore (10), can operate at least between a continuous input element and a continuous output element of the coke. In addition to operating to raise by drill the material, the inclination of the container (5) of the process can serve to force the coke out of container (5) of the process. As can be appreciated, the movement element can serve to grind, weave, drill, cut, break or otherwise cause the formed coke to be forced out of the container (5) of the process. Importantly for a modality, the removal of coke can occur while forming coke due to the heating of the material. You can present a continuous removal process, as desired, in some modalities. The coke, remaining material, or other residue can then exit the pyrolyzer (1) to an exit of the remaining material, such as the outlet (4) of the waste. Being able to present a continuous process,. the remaining residue or material may be especially suitable for disposal.

Depending on the initial material processed and the configuration of the system, it may still have a substantially coked residue (ie, more than 80%, 85% 90%, 95% or even 98%) all of a volatile organic material or residue. Thus, by the time the matter leaves the pyrolyzer, almost all the volatile hydrocarbon can be removed and only inorganic solids and petroleum coke can remain. Even the remaining coke may be more appropriate for disposal. A system, according to one embodiment of the present invention, can remove continuously creating coke, which has no more than 6.7% d sulfur content or which has not yet more than 3.7% d sulfur content. Thus, the screw or drill (10) can serve as a continuous coke exit element and the system can operate to form coke out of an organic, substantially non-volatilized material. Obviously, when the system can be designed so that the source of heat of coke formation operates to coke substantially all of the residue, an optimum situation can exist. To understand how the screw or drill (10) can serve as a continuous coke production element, it should be appreciated that such an arrangement is a way to configure the system. As an ordinary expert in the art will readily appreciate, many other ways are possible, including, but not limited to, using a coke grinding element, a coke abrasion element, a coke bore element, an element d Coke cutting, a breaking element of coke, or many other types of elements. Importantly from the efficiency perspective, the output element can be operated while the heat source of the coke formation acts to form the coke and can serve as a continuous output element of said coke, to which the remaining material is responsive. Again the tilted screw arrangement is merely a representative design. To promote the desired heat transfer, the pyrolyzer (1) may include a fluidized bed of hot sand, such as the sand bed (15), as the high conductive energy transfer element. As is well known, the sand bed (15) can have a gas supply (18) to increase the conduction. The rotating screws can be submerged in the bed. The incoming material that is going to be processed can be fed into these screws and borne into the hot zone of the pyrolizer. As the material heats up inside the screw, can develop light hydrocarbon vapors, which can be removed, condensed and recovered as a liquid hydrocarbon product. The system can then achieve the production of the waste material or the coke through the outlet (4) of the waste. The remaining coke can be discarded. Using the bed (15 sand as the energy transfer element) can facilitate the appropriate process, for example, the heat can be transferred to a regime to properly establish a first thermal environment within which the material can be processed. A second thermal environment, which differs from the first environment, heat can be transferred differentially, for example, by establishing a liquid conduction medium there can be more heat condensation in this environment than in the gaseous conduction environment. High conductivity, which can be effective over an effective process length (as an example a length in which refining occurs and significantly influenced by the heat source) can thus be coordinated with one or more refinery characteristics (for example , heat transfer heat d, screw speed, heat supply amount etc.) to prese ntar an optimal system. As mentioned, the pyrolyzer can use a fluidized bed of hot sand in which the rotating screws are immersed, however, this should be understood only as a type of design that conducts highly energy.

In embodiments that use a tilt, the material can move at an inclination, such as that shown exists within the container (5) of the process as it moves from the entrance (2) to an exit. Thus the system can present an inclined refining process area. Correspondingly, there may be an inclined movement element to which the material is sensitive, such as an inclined screw or bore element (19) illustrated within the inclined refining process area. The inclination can also serve to create a seal between the volatile matter and the entrance (2). As shown, the pyrolyzer (1) can have a higher part (16) of the entry end, and a bottom end portion (17), which differ in level height. This can be used to create a totally liquid area and a totally gaseous area, to facilitate sealing. The amount of the tilt can vary with the quantity and type of material being processed, the geometry of the system and other factors. As an example, an angle d at least: 15 °, 22.5 °, 30 ° and 45 °, can serve to achieve the desired sealing and refining operations. In addition, all that may be necessary is that the part of the fund (17) of the outlet end may be substantially greater than the upper part (16) of the inlet end, so that the subsequent blowing of the volatile matter does not occur.

Additionally, the inclination must not be so steep that the coke or other remaining material can not pass above the inclination through the motion element operation, such as the drill screw element (10). Thus the element of movement can serve as an element of movement that overcomes the inclination, creating refined products perhaps through all that element moves in a way that exceeds the effects of the inclination. The bottom part (17) of the outlet end may still be substantially above the liquid level d, so once a certain coke can be removed only and not the unprocessed material. In such a configuration, the production of the unit can also be determined by any reaction kinetics or the heat transfer rate. Since the lower portion of the screw can be filled with liquid, the transfer of heat in this region can be rapid on the side of the process and can be controlled by convective heat transfer on the gas side of the screw. The use of a fluidized bed on the side of the gas can also lead to very rapid transfer of heat to the screw, thus, in service the production of the pyrolyzer can be controlled by the kinetics of the coking reactions. The length, speed and other parameters of the process can thus be based on a variety of factors, including but not limited to the amount of heat transfer in the apparatus, the speed at which said apparatus is operated, the amount of heat supplied to the apparatus, the amount d heat transfer in the gaseous conduction environment, the amount of heat transfer in the d transfer element of high conduction energy, the kinetics of the coking reactions occurring within the refinery apparatus, etc. Through the provision of an inclined process area, an advantage in sealing the system can be achieved. As shown in Figure 1, the upper part (16) of the inlet end of the pyrolyzer (1) is larger than the bottom part (17) of the outlet end. This can be appreciated from the level line (19), which represents the level that the liquid would tend to achieve under the static conditions. Depending on the speed at which the screw or drill (10) operates, some liquid can, of course, achieve a higher level towards the bottom end portion (17). In a coking mode, a met can be to prevent it from reaching the outlet (4) of the waste, so that only the coke or other residue leaves the system. This can be achieved by the inclination that creates a totally gaseous area at the end. of exit. furtherThe inclination can serve to create a totally liquid area at the inlet end to facilitate the sealing of the volatile matter present in the output (3) of volatile material, to push backwards and out of the inlet (2). Very similar to a liquid trap, the tilt is a way to establish a liquid seal between the inlet (2) and the outlet. Instead of providing a separate element to achieve sealing, the present invention uses at least some of the material to be processed with a more efficient system. A variety of sealing levels are possible, of course, including, but not limited to at least a seal of about 0.07 kg / cm2, at least a seal of about 0.14 kg / cm2, a seal having at least 61 cm of liquid or depth column, a seal that has at least 30.5 cm of liquid column, a seal located around the middle between the inlet and the outlet, and an adequate seal to avoid the subsequent blowing of the results from the volatile substances. As can be appreciated, the seal can be established at an interface between the material and the volatilized substances. When the stamp is created, the tilt serves to establish a seal creation of the inclined refining process area. It also consists of and uses the hydrocarbon entry or material. As those skilled in the art will readily understand, the material to be refined by the pyrolyzate (1) can be treated before going inside the pyrolyzer (1) and after leaving this pyrolyzer (1). Such element stages are shown schematically in Figure 4. In the broad sense, the pre-treatment step of the material, of course, occurs before achieving the continuous volatilization of substances and can be achieved by one or more types of a device (20). ) of previous treatment. Some types of functions that may be used include, but are not limited to: heat treatment, flash vaporization, separation and the various permutations and combinations of these and other steps. Considering the pyrolyzer (1) as the focus refinery apparatus, this apparatus is responsive to the various pre-treatment elements if they are a thermal treatment device, vaporizer, separator, or the like. As shown in Figure 4, both a vaporized (21) and a separator (22), used in this embodiment, are shown. As can be seen from Figure 4, the flux of the material is from a source of a non-processed material (23) to the outlet (13) of the refined product. As part of a particular pre-treatment (20) illustrated, both a vaporizer (21) and a separator (22) are used. The separator (22) can be an atmospheric distillation unit, with the solids agitated by a gas of the separates swept, provided through the supply (24) of the separator sweep gas, to bubble through the element. The nature of the oil or other hydrocarbon fed to the separator (22) (particularly its curve of boiling point and specific gravity) can have a significant influence on the amount of product removed from the separator (22) at the outlet (25) thereof, as well as the pyrolyzer (1), and the quality of that product. Due to the variation of the operating temperature of the separator (22), higher or lower quantities of distillation can be produced in the upper part, with the rest being reported with the residue from the separator bottoms, these separator bottoms can be fed to the pyrolyzer (1). Using the Cold Lake crude as an example, it was estimated that approximately 55% of the crude will be recovered as distilled from the separator as a 20.2 ° API oil having a sulfur content of 2.9 percent by weight. Then the refined product that comes out of the pyrolyzer (1 can be a light distillate, free of residue, with an API gravity in the range of 25 to 60 °) The entire operation of the separator can, of course, be varied.This can include a variety of stages, which include, but are not limited to: atmospheric distillation, bubbling of a gas swept through the material, both atmospheric distillation and the bubbling of a sweeping gas through the material, creating at least some of the same material 20 ° API, create at least some of the same material of 60 ° API, the permutations and combinations of each of them. Thus the separator (22) can include an atmospheric distiller and a sweep gas feed (24), and both of them. As shown in Figure 4, the device (20) Pretreatment may also include element to evaporate the material. This is n generically as the vaporizer (21). As summarized in Figure 5, the feed to a type of the process material may consist of a mixture of suspended oil, water and solid. In processing such material, the mixture can first be heated under pressure to temperatures near 204 ° C, and then expanded through the evaporation valve to atmospheric pressure. This is a type of evaporation with a sudden drop in pressure, to release emulsified water as water vapor. This can be discharged without damage to the chimney (26). The hot evaporation funds can then be sent to the separate (22), where the first oil product or other refined product can be recovered. The act of evaporating the material can, of course, be achieved before performing the stage of continually volatilizing the substances. It can also be varied greatly and can include the steps of: heating the material to at least about 204 ° C, quickly reducing the pressure of the material heated to approximately atmospheric pressure, and both of them. The unit, illustrated generically as the evaporation device (21) then produces at least some of the heavy hydrocarbon material for the refining apparatus. Thus the elements used can include a heat source which operates to achieve a material temperature of about 204 ° C, a pressure reducer generically an atmospheric vaporization device. The treatment of the refined products of pyrolyzer (1) can also be included. As n, this can be achieved generically by the device (11) d treatment after refining. As its name implies, it can be configured to allow the subsequent treatment after the refined pyrolyzer products (1) are created and can be located or before the condenser (12). At least some of the volatilized substances can be fed into it and thus the treatment device (11) after refining can be responsive to the refinery apparatus. A type of treatment after refining may be hydrotreatment, such as where the device (11) d treatment after refining includes or serves as a hydrotreatment. The graph of Figure 3 is a summary of some hydrotreating results obtained in the upper part of the pyrolyzer in the example. The sample labeled "Untreated 2", and the label "Petróle del Separador", are the samples discussed before. The remaining samples were generated during a test from the original material labeled "Untreated 1". The number of bromine and the value of diene by the maleic anhydride, are empirical indications of the presence of olefins (bromine number) and conjugated dienes (dienes by maleic anhydride). The value of the maleic anhydride did not directly reflect the concentrations of the dienes in the sample, because the mass of each individual sample the titration molarity is required for this calculation. Similarly, the value of the diene is an indication of the conjugated double bonds and it is subject to the interferences of species such as anthracene and other aromatic polyhydrocarbons, which are abundant in these oils. As a result, the absolute meaning of these values must be interpreted with caution. The hydrotreatment achieved in this example is hydrotreatment of the refined products at least around 126 kg / cm2, through a pressure element. (illustrated as part of the pretreatment device capable of achieving that pressure.

Figure 3 s that hydrotreating at 126 kg / cm can lead to low hydrogen consumption, concentration of olefins significantly reduced or eliminated, an acceptable H / C ratio, and operating conditions that lead to a maximum catalyst life. If some residual olefins remain they may not be highly reactive and probably will not need to be saturated in order to prevent the formation of gum. further, the extreme case of thermal decomposition and the subsequent re-saturation suggests an alternative configuration where all the material is first sent to the pyrolyzer and then hydrotreated to produce maximum amounts of light oil product for the replacement of condensate, mixing and sale. Efficient energy utilization and hydrogen management can be valuable for self-sustaining design thermal efficiency and low operating costs. The pyrolyzer can produce a light hydrocarbon oil which, once stabilized, can contribute significantly to the value of the general product. The hydrogen required to achieve this stabilization and to hydrotreat the upper fraction of the additional separator may also be derived from the coking of a portion of the bottoms of the separator. In doing so, suitable petroleum coke for the combustion of the pyrolyzer can be produced. The remaining products, hydrocarbons Ci to C6, can be sold as products.

Generally, all the material that enters can be converted into high value products or consumed as fuels. On an exempt basis of BS & W, the process in example can be configured to be able to recover approximately 80 to 85% of the original hydrocarbon as a product oil with the remaining material divided between the process fuel gas and the coke. On a general process basis and as an example, the Cold Lake crude process with the present process of the invention can produce 16,404 bpd of 26.5 ° API of petroleum product containing 3.67% sulfur, 712 tons per day of coke that it contains 6.7 $ of sulfur, and 6.18 MM scf / day (0.175 M m3 / day) of fuel gas with an HHV of 1328 Btu / scf (118 K-calories / m3). Of course, these stages of the process have applications similar to those of a modern refinery. As a result, the technology, with variations appropriate improvements, is ideally suited for development in the oil fields as a mobile, modular refinery, manufactured in the workshop. For further efficiency, the system can be designed to return some or all of the energy needed to operate the process. It can be self-sustaining using the energy generated from the refined products in the refining method. This can be achieved by burning the non-condensable refined products generated in the method among other returns. Thus the system can use substantially no input energy for energy supply to the stages of the refining method. In the schematic view of Figure 4, the element (27) d energy reuse is conceptually shown using some of the production (25) of the separator to return energy to the refinery apparatus (illustrated as returning as heat input to the pyrolyzer (1).) It may also be directed to the use of some combustion element of the non-condensable refined products (illustrated as part of the element of energy reuse) to facilitate the return of energy.

Example of plant: Bitumen Cold Lake. An example the plant d 20,000 b / d processed Cold Lake bitumen, an 11 ° API crud, containing 4.6% sulfur was used to illustrate the principles involved in an approach Improvement of this crude could produce 16,404 bp (barrels per day) of a 26.5 ° API product containing 3.1% sulfur by weight. The plant can also produce 712 tonnes / day of coke (6.74% S) and 6.2 MM scf / day (0.17556 MM m3 / day) d fuel gas having an HHV of 1328 Btu / scf (118 k-cal / m3). The facility may require no energy or fuel imports and will probably have an operating cost (excluding charges related to the capital) of less than Cdn $ 0.65 / barrel (0.6 Canadian dollars per barrel). The capita costs for such an installation and the like may be determined in association with the heavy oil producers and the assignee of the present invention. However, based on experience estimates from the National Center for Upgradin Technology in Devon, Alberta, Canada, a total capital investment of Cdn $ 98.2 million for the facility and an operating cost, which includes capital costs, of Cdn $ 2.66 per barrel, it can be achieved. Of this, $ 2.02 are charges relative to the capita and thus the figure of this nature can be included equally. In this example, the process can also be configured to produce coke and fuel gas and can be used regardless of energy.

Although a different application, drilling muds and other problematic materials can be processed equally. In an energized system, the gas and electricity charges can be approximately $ 3.25 / ton assuming energy at 0.05 / kh and natural gas at $ 2.25 / Mcf. As much as 112.55 liters of diesel oil can be recovered per tons of processed material. This has been credited to the process at $ 10 / ton after allowing solid waste to be disposed of by land filling with labor from the operation, assuming it is $ 40 / hour for two operators / displaced on the clock. Capital charges can be estimated at 15% of the total capital investment. Although preliminary, these economies suggest that process charges of $ 3O / ton or less should be possible for reasonable intervals of specific capital investment and for reasonable plant operating factors. In this different type of application, that is, not for the continuous refining of the heavy oil supplied, but rather for the thermal removal of hydrocarbons from the drilling mud or other waste products, the heat transfer can be arranged for be fast from the fluidized bed to the screw cover and vaporization can be instantaneous once the evaporation temperatures are reached. In this case, the material in the screw can be either a mud or a wet solid with a coefficient d lateral heat transfer of the resulting process which can be considerably less than that of the previous cas. Here, the overall production can be controlled by the heat transfer regime from the casing of the inclined screw to the inner mass of the humid solid on the side of the process. Such individual heat transfer coefficients d and their effects any process or general heat transfer may need to be measured experimentally. Thus, it can be seen that the present invention can be applied to, but not limited to, heavy oils of crude oils any other mixture of hydrocarbon products, water, sediments. Although perhaps of less commercial significance, it can be used to transform waste materials, such as waste from tank bottoms and drilling mud. Such use of some components of the present invention may be for the recovery of waste material, as discussed in U.S. Patent No. 5,259,945, incorporated herein by reference. This process, referred to as the process "RaBoRR" - (trademark of the transferee), is a process of recovery of distillate oil and improved mixtures of petroleum, water sediments. The process economy of these drilling muds or the like in a pyrolyzer of the present invention was preliminarily estimated in the graph of Figure 3. The specific inversion of the capital may depends on the heat transfer coefficients, determined during the experimental program , but it is expected to vary between 0.1 to 1 $ MM / ton / hour.

As can be easily understood from the foregoing, the basic concepts of the present invention can be incorporated in a variety of ways. It involves both refining techniques and devices to achieve proper refining. In this application, the refining techniques are described as part of the results shown that will be achieved by the various devices described and as stages which are inherent in the use. As a few examples, refining techniques can be used in, but not limited to, the improvement of heavy oils, tar sands process production, refining of crude oil and other small and large refineries. There is simplicity in the natural result of using the devices as intended. In addition, while some devices describe, it will be understood that they not only achieve certain methods, but can also be varied in a number of ways. Importantly, according to the above, all facets must be understood to be achieved by this description. The discussion included in this patent intends to serve as a basic description. The reader should be aware that the specific discussion may not explicitly describe all possible modalities, and many alternatives are implicit. It may also not fully explain the generic nature of the invention and may not explicitly show how each characteristic element may actually be representative of a broader function or of a great variety of alternative equivalent elements. Again, there is implicity included in this description. When the invention is described in the terminology oriented to the device, each device element implicitly executes a function. The claims of the apparatus may not be included for the described device, but also the claims of the method or process may be included to direct the functions of the invention and that each element executes. Neither the description nor the terminology attempt to limit the scope of the claims available to the applicant. It should also be understood that a variety of changes can be made without departing from the essence of the invention. These changes are also implicitly included in the description. They are still within the scope of this invention. An extensive description that encompasses both the explicit modalities shown, the great variety of implicit alternative modalities, as well as the broad and similar methods or processes, is covered by this description. It should be understood that such a description may cover numerous aspects of the invention, both independently and as a general system.

Furthermore, unless the context requires it otherwise, it should be understood that the term "comprise" variations, such as "comprises" or "understanding", is intended to imply the inclusion of a designated element or stage or group of elements or stages, but not the exclusion of any other element or stage or group of elements stages. These terms must be interpreted in their most extensive form, in order to provide the applicant with the broadest coverage that can legally be allowed. In addition, each of the various elements of the invention and the claims can also be achieved in a variety of ways. This description should be understood to cover every variation, whether it is a variation of a modality of any modality of the apparatus, a modality of a method or process, or even merely a variation of any element of them. Particularly, it should be understood that the description refers to element of the invention, the words for each element can be expressed by equivalent terms of apparatuses or methods -even if only the function or result is the same. Such an equivalent, broader, or even more generic term should be considered covered in the description of each action element. Said terms may be substituted where desired to make explicit the implicitly extended coverage to which this invention is entitled.

As an example, it must be understood that all actions can be expressed as a means to take that action as an element which causes that action. Similarly, each physical element described must be understood covering a description of the action which facilitates said physical element. Regardless of this latter aspect, as an example, the description of a "separator" should be understood to encompass the description of the act of "separation" explicitly discussed or not - and, conversely, where only the act of "separation" is described. ", such description must be understood encompassing the" separator "and even a" half separation ". These terms of changes and alternatives must be understood as explicitly included in the description. In addition, as each term used must be understood that, unless its use in this application is inconsistent with such interpretation, the common definitions of the dictionary should be understood as incorporated in each term, and all definitions of alternative terms and synonyms, such such as the contents of the Random House Webster 's Unabridge Dictionary, Second Edition, are here incorporated with reference. Finally, all the references in the description or listed in the References list, will be incorporated presented with the application and are appended here as reference, as in the previous priority application, US Requests. We 60 / 167,335 and 60 / 167,337 (with their incorporated references) any other reference mentioned in the application for this patent, like all references listed and any list that is incorporated, presented with the present and / or previous application, are incorporated with reference in its entirety. However, when extensive declarations may be considered inconsistent with the patentability of these inventions, such statements will not be considered expressly made by the applicants. Additionally, the requests must be understood as support to claim the various combinations and permutations of each of the elements described.

LIST OF REFERENCES US PATENT DOCUMENTS FOREIGN PATENT DOCUMENTS OTHER DOCUMENTS Patent Application of the United States of America, No. 60 / 167,337, "Apparatus Methods to Improve Heavy Petroleum", presented on November 24, 1999 U.S. Patent Application No. 60 / 167,335, "Methods of Apparatus for the Improved Pyrolysis of Hydrocarbon Products", filed on November 24, 1999. U.S. Patent Application No. 60 / 138,846 , "" Predeci Proximidad a la Formacion de Coque ", presented on June 10, 1999.

Claims

CLAIMS 1. A method for refining heavy hydrocarbon material, this method comprises the steps of: a) continuously entering a material containing at least some heavy hydrocarbon material; b) heating said material; c) continuously volatilize substances of said material, to form refined products; d) collecting at least some of said refined product, - e) substantially exceeding the temperature of coke formation, within said material; f) forming the coke from some of said material and g) continuously removing said coke. 2. A method for refining heavy hydrocarbon material, as described in claim 1, wherein said step of substantially exceeding the coke formation temperature within said material comprises the step of achieving at least one temperature selected from the group consisting of: 343 ° C 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C. 3. A method for refining heavy hydrocarbon material, as described in claim 2, wherein the step of continuously entering a material containing at least some heavy hydrocarbon material, comprises the step d continuously entering material selected from the group that consists of: heavy oils, asphalt, tar, bitumen, material having an API gravity of less than approximately 11 ° API, material having an API gravity of less than about 10 ° API, material having an AP gravity of less than about 7 ° API , material having an API gravity of less than about 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material which it has at least 10% by weight of waste, and material that has less than 15% by weight of waste. 4. A method for refining heavy hydrocarbon material, as described in claim 2, wherein said step of forming the coke, starting from at least some of said material, comprises the step of forming a substantial amount of coke from said material. 5. A method for refining heavy hydrocarbon material, as described in claim 4, wherein said step of forming a substantial amount of coke from said material comprises the step of forming a quantity of coke from said material, selected from the group consisting of of at least about: 1% by weight of said input material of the coke material, 2% by weight of said input material of the coke material, 5% by-weight of said input material of the coke material , 10% by weight of said input material of the coke material, 20% by weight of said input material of the coke material, 44% by weight of said input material of the coke material. 6. A method for refining heavy hydrocarbon material, as described in claim 4, wherein said step of forming a substantial amount of coke from said material comprises the step of forming the coke from substantially all of the non-volatilized organic material. 7. A method for refining heavy hydrocarbon material, as described in claim 4, wherein said step of forming a substantial amount of coke from said material comprises the step of forming the coke of substantially all of the residue. 8. A method for refining heavy hydrocarbon material, as described in claim 2, further comprising the step of moving at least some of the material from the inlet to the outlet. 9. A method for refining heavy hydrocarbon material, as described in claim 2, wherein said step of continuously removing the coke comprises a process selected from the group consisting of: grinding the coke, abrading the coke, treating the coke by drill , cut the coke and break the coke. 10. A method for refining heavy hydrocarbon material, as described in claim 2, wherein the step of continuously removing the coke occurs while achieving the step of forming the coke from at least some of said material. 11. A method for refining heavy hydrocarbon material, as described in claim 2, further comprising the steps of: a) establishing a first thermal environment, within which the material is processed; and b) establish a second thermal environment, within which the material is also processed. 12. A method for refining heavy hydrocarbon material, as described in claim 11, wherein said step of establishing a first thermal environment, within which the processed material comprises the step of establishing a liquid driving environment, and wherein the stage of establishing a second thermal environment, within which the material is also processed, comprises the stage of establishing a gaseous conduction environment. 13. A method for refining heavy hydrocarbon material, as described in claim 2, further comprising the step of moving said material at an inclination from the entrance to an exit. 14. A method for refining heavy hydrocarbon material, as described in claim 2, further comprising step d establishing a liquid seal between an inlet and an outlet. 15. A method for refining heavy hydrocarbon material, as described in claim 14, wherein the step of establishing a liquid seal, between an inlet and an outlet, comprises the step of using at least some of the material that contains at least some of heavy hydrocarbon material. 16. A method for refining heavy hydrocarbon material, as described in claim 15, wherein the step of establishing a liquid seal, between an inlet and an outlet, comprises the step of establishing a liquid seal selected from the group consisting of : a seal of at least about 0.0 kg / cm2, a seal of at least about 0.14 kg / cm2, or seal having a liquid column of at least 61 cm, or seal having a liquid column of at least 30.5 cm a seal placed around half way between an entrance and an exit, a suitable seal to avoid the subsequent blowing of the results of said stage to continuously volatilize the substances. 17. A method for refining heavy hydrocarbon material, as described in claim 2, wherein the step of collecting some of said refined products comprises the step of condensing at least some of the results of said step of continuously volatilizing the substances. 18. A method for refining heavy hydrocarbon material, as described in claim 17, wherein said step of collecting at least some of the refined products, comprises step d collecting the refined products having an AP gravity selected from the group consisting of at least approximately 25 ° API, up to at least approximately 60 ° API. 19. A method for "refining heavy hydrocarbon material, as described in claims 2, 11, 13, 14 or 17, further comprising the step of pretreating said material containing at least some heavy hydrocarbon material, before performing the stage of continuously volatilizing the substances from said material, to form refined products. 20. A method for refining heavy hydrocarbon material, as described in claim 19, wherein said step of the pretreatment of the material containing at least some heavy hydrocarbon material, before performing step d, continuously volatilizes the substances of said material. to form refined products, comprises the etap selected from the group consisting of: the thermal treatment of said material, instant vaporization of said material, separation of said material, and the permutations and combinations of each of the above. 21. A method for refining heavy hydrocarbon material, as described in claim 19, wherein the step of pretreating material containing at least some heavy hydrocarbon material., before carrying out stage d continuously volatilize the substances of said material, to form refined products, it is selected from the group consisting of: atmospherically distilling said material, bubbling a sweeping gas through said material, both atmospherically distilling said material to bubble a scavenging gas through said material, create at least some material of about 20 ° API, create at least some material of approximately 60 ° API, permutations and combinations thereof. 22. A method for refining heavy hydrocarbon material, as described in claims 2, 19 or 20, further comprising the step of evaporating the material before performing said step d continuously volatilizing substances from said material, to form refined products. 23. A method for refining heavy hydrocarbon material, as described in claim 22, wherein said step of evaporating the material, before performing the step of continuously volatilizing the substances of said material, to form refined products, is selected from the group that it consists of heating said material to at least about 204 ° C, rapidly reducing the pressure of said heated matter to about atmospheric pressure, and heating said material to at least about 204 ° as rapidly reducing the pressure of said heated matter to about atmospheric pressure. 24. A method for refining heavy hydrocarbon material, as described in claims 2 or 19, further comprising step d treating said refined products later, after they are created. 25. A method for refining heavy hydrocarbon material, as described in claim 24, wherein said step of subsequently treating said refined products, after they are created, comprises the step of hydrotreating said refined products, after they are created. 26. A method for refining heavy hydrocarbon material, as described in claim 25, wherein the step of hydrotreating said refined products, after they are created, comprises the step of hydrotreating said refined product to at least about 126 kg / cm2. 27. A method for refining heavy hydrocarbon material, as described in claim 25, further comprising the steps of: a) condensing at least some of the results of said step of continuously volatilizing the substances; and b) pre-treating said material, which contains at least some of the heavy hydrocarbon material, before carrying out the step of continuously volatilizing the substances of said material, to form refined products, selected from a group consisting of: the thermal treatment said material,. evaporation of said material, separation of said material, and the permutations combinations of each of the above. 28. A method for refining heavy hydrocarbon material, as described in claims 2, 11, 13, 14, 17, 19, 22 or 24, which further comprises the step of using the energy generated from said refined products, in said method of refinement. 29. A method for refining heavy hydrocarbon material, as described in claim 28, wherein said step of using the energy generated from said refined products in said refining method, comprises the step of burning the non-condensable refined products, generated in said method. 30. A method for refining heavy hydrocarbon material, as described in claim 29, further comprising the step of using substantially input energy to energize the steps of said refining method. 31. A method for refining heavy hydrocarbon material, as described in claim 29, wherein the step of collecting at least some of said refined products comprises step d condensing at least some of the results of said step of continuously volatilizing the substances, and further comprises the step of previously treating said material containing at least some of the heavy hydrocarbon material, before achieving said step of continuously volatilizing the substances from said material, to form refined products, by performing a stage selected from the group consisting of : the thermal treatment of said material, evaporate said material, separate material, and the permutations and combinations of each of the above. 32. A method for refining heavy hydrocarbon material, as described in claim 2, wherein the step of continuously entering a material containing at least some of the heavy hydrocarbon material, comprises step d continuously entering a material having a API gravity of at most approximately 11 ° API. 33. A method for refining heavy hydrocarbon material, as described in claim 2, wherein the step of continuously removing the coke comprises the step of continuously removing the coke selected from the group consisting of: coke having no more than about 3.7 % sulfur content coke having no more than about 6.7% d sulfur content. 34. A method for refining heavy hydrocarbon material, as described in claim 2, wherein said refined products have characteristics selected from a group consisting of: an API gravity of at least about 26 ° API, no more than about 3.7% of sulfur content, no more d approximately 3.1% sulfur content, the characteristics of a combustible gas, and the permutations combinations of each of the above. 35. An apparatus for the continuous refining of coke, this apparatus comprises: a) a continuous input, adapted to continuously accept material containing at least some heavy hydrocarbon material; b) a source of heat of formation of the coke, to which said material is sensitive, which causes the substances to emit volatilized substances from said material, and cause the substantial formation of coke from at least some of the material; c) an output of volatiles, which is adapted to receive at least some of said volatilized substances and d) a continuous output element of the coke. 36. An apparatus for the continuous refining of coke, as described in claim 35, wherein said heat source of the coke formation to which said material is sensitive, comprises a coke formation heat source, which substantially exceeds The temperature of formation of the coke within said material, selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C. 37. An apparatus for continuous refining of the coke, as described in claim 36, in which continuous input, adapted to continuously accept the material containing at least some of the heavy hydrocarbon material, acts on at least some of the material selected from the group that consists of: heavy oils, asphalt, tar, bitumen, material having a severe API less than about 11 ° API, material having an API gravity of less than about 10 ° API, material having an API gravity of less than about 7 ° API , material having an API gravity of less than about 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material which has at least 10% by weight of waste, and material that has at least 15% by weight of waste. 38. An apparatus for the continuous refining of coke, as described in claim 36, wherein the heat source of the coke formation to which said material is sensitive comprises a coke formation heat source operating to form a coke. substantial amount of coke from said material. 39. An apparatus for the continuous refining of coke, as described in claim 38, wherein the heat source of the coke formation, which operates to form a substantial amount of the coke from said material, is configured to operate to form a quantity of coke from said material, selected from the group consisting of at least about: 1% by weight of said input material of the coke material, 2% by weight of said input material of the coke material, 5% by weight weight of said input material of the coke material, e 10% by weight of said input material of the coke material, 20% by weight of said coke material input material, and 44% by weight of said material d input of the coke material. 40. An apparatus for the continuous refining of coke, as described in claim 38, wherein the heat source of the coke formation, which operates to form a substantial amount of the coke of said material, comprises a heat source forming a coke. coke, which operates to form coke of substantially all non-volatilized organic matter. 41. An apparatus for the continuous refining of coke, as described in claim 38, wherein the heat source of the coke formation, which operates to form a substantial amount of coke from said material, comprises a source of heat of formation. coke, which operates to form coke of substantially all the residue. 42. An apparatus for the continuous refining of coke, as described in claim 36, further comprising a movement element, which operates at least between said continuous input element and said continuous output element of the coke. 43. An apparatus for the continuous refining of coke, as described in claim 42, wherein said movement element, which operates at least between said continuous input element and said continuous output element of the coke, comprises a moving element selected from the group that consists of crushing the coke, l abrasion of the coke, treat the coke by drill, cut and coke and break the coke. Four . An apparatus for the continuous refining of coke, as described in claim 36, wherein said continuous coke outlet element operates while said coke-forming heat source acts to form this coke. 45. An apparatus for the continuous refining of coke, as described in claim 36, further comprising: a) a first refining environment, within which the material is processed; and b) a second refining environment, within which the material is processed. 46. An apparatus for the continuous refining of coke, as described in claim 45, wherein said first refining environment comprises a liquid conduction environment d and wherein said second refining environment comprises a gaseous conduction environment. 47. An apparatus for the continuous refining of coke, as described in claim 36, further comprising: a) an inclined area of the refining process, within which at least some of said material and less some of said volatilized substances are contained; and b) an inclined movement element, to which material is responsive within the inclined area of the refining process. 48. An apparatus for the continuous refining of coke, as described in claim 36, further comprising a liquid seal, established at an interface between said material and said volatilized substances. 49. An apparatus for the continuous refining of coke, as described in claim 48, wherein said liquid seal is established at an interface between said material and said volatilized substances comprises a heavy hydrocarbon material. 50. An apparatus for the continuous refining of coke, as described in claim 49, wherein the liquid seal comprises a seal selected from the group consisting of: at least one seal of approximately 0.0 kg / cm2, at least one seal of approximately 0.14 kg / cm2, or seal that has at least 61 cm of liquid column, or seal that has at least 30.5 cm of liquid column, or seal placed approximately mid way between an inlet and outlet, an adequate seal to avoid the subsequent blowing of the refined material. 51. An apparatus for the continuous refining of coke, as described in claim 36, further comprising a capacitor responsive to the refining apparatus to which at least some of the volatilized substances are fed. 52. An apparatus for the continuous refining of coke, as described in claims 36, 45, 47 or 51, further comprising a pre-treatment device, to which said refining apparatus is sensitive, which produces at least some of the material of heavy hydrocarbons for said refinery apparatus. 53. An apparatus for the continuous refining of coke, as described in claim 52, wherein said pretreatment device comprises an apparatus selected from the group consisting of a thermal treatment device, an evaporator, a separator, and the permutations and combinations of each of the above. 54. An apparatus for the continuous refining of coke, as described in claim 52, wherein the pre-treatment device comprises an apparatus selected from a group consisting of: an atmospheric distillate, a sweeping gas feeder, and both distiller atmospheric as a gas feed swept d. 55. An apparatus for the continuous refining of coke, as described in claims 36, 52, 53, which further comprises a vaporizer, to which the refining apparatus is sensitive, and which produces at least some heavy hydrocarbon material for said apparatus. refinement. 56. An apparatus for the continuous refining of coke, as described in claim 55, wherein said vaporizer, to which the refining apparatus is sensitive, and which produces at least some of the heavy hydrocarbon material, for said refining apparatus comprises a apparatus selected from the group consisting of a heat source, which operates to achieve a material temperature of at least about 204 ° C, a pressure reduction, an atmospheric evaporator and the permutations combinations of each of the above. 57. An apparatus for the continuous refining of coke, as described in claims 36 or 52, further comprising a treatment device after refining, responsive to said refining apparatus to which at least some of the volatilized substances are fed. 58. An apparatus for the continuous refining of coke, as described in claim 57, wherein said refining treatment device, responsive to said refining apparatus and to which at least some of said volatilized substances are fed, comprises a device of hydrotreating. 59. An apparatus for the continuous refining of coke, as described in claim 58, wherein said hydrotreating device comprises a pressure element, capable of achieving a pressure of at least 12 kg / cm2. 60. An apparatus for the continuous refining of coke, as described in claim 58, further comprising: a) a condenser, responsive to said refining apparatus and to which at least some of the volatilized substances are fed; and b) a pre-treatment device, to which a refining apparatus is responsive, and which produces at least some of the heavy hydrocarbon material for said refining apparatus and selected from a group consisting of: a thermal treatment device, an evaporator, a separator and the permutations and combinations of each of the above. 61. An apparatus for the continuous refining of coke, as described in claims 36, 45, 47, 48, 51, 52, 55 or 57, which further comprises an energy reuse element, which returns energy to said refining apparatus . 62. An apparatus for the continuous refining of coke, as described in claim 61, wherein said energy re-use element, which returns energy to said refining apparatus, comprises a combustion element of the non-condensable refined products. 63. An apparatus for the continuous refining of coke, as described in claim 62, further comprising: a) a condenser, responsive to the refining apparatus and to which at least some of the volatilized substance is fed; and b) a pre-treatment device, to which a refining apparatus is responsive and which produces at least some of the heavy hydrocarbon material for said refining apparatus and selected from a group consisting of: a thermal treatment device, an evaporator, a separator and the permutations and combinations of each of the above. 64. A refinery apparatus for the differential process, said apparatus comprises: a) an input to a process container, adapted to continuously accept material, in which material contains at least some of the heavy hydrocarbon material; b) a source of heat, to which said responsive material, which causes volatilized substances to be emitted from said material; c) a first refining environment, inside the process container, and within which the material is processed; d) a second refining environment, inside the process container and within which the material is processed; e) an output of volatiles, which is adapted to receive at least some of the volatilized substances; and f) an exit of the remaining material. 65. A refinery apparatus, of differential process, as described in claim 64, and said heat source to which said sensitive material, comprises a heat source which achieves a material temperature of at least one selected from the group. consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C 510 ° C, 538 ° C, 593 ° C and 648 ° C, and in which said input continuously accepted at least some of the heavy hydrocarbon material, selected from the group consisting of: heavy oil, asphalt, bitumen tar, material having API gravity less than 11 ° API, material having API gravity less than 10 ° API, material having an API gravity less than 7 ° API, material that has a gravity. API less than 3 ° API, material that has a lot of waste signatures, material that has at least 5 weight of waste, material that has at least 7% weight of waste, material that has at least 10% in waste weight, and material that has at least 15% by weight d waste. 66 A refinery, differential processing apparatus, as described in claim 64, further comprising a third refining environment within which the material is processed. 67. A refinery apparatus, of differential processing, as described in claim 66, and said third refining environment, within which the material is processed, comprises a combination of the first second refining environment. 68. A refinery apparatus, of differential processing, as described in claim 66, and wherein the third refining environment, within which the material is processed, comprises a refining d environment. 69 A refinery, differential processing apparatus, as described in claim 68, wherein said transition refining environment comprises a transition refining environment selected from the group consisting of: a gradual transition environment and a linear transition environment. 70. A refinery apparatus, of differential processing, as described in claim 64, wherein said first refining environment comprises a first thermal environment, and wherein said second refining environment comprises a second thermal environment. 71. A differential processing refinery apparatus, as described in claim 66, wherein said first refining environment comprises a first thermal environment, wherein the second refining environment comprises a second thermal environment, and wherein the third refining environment comprises a third thermal environment. 72. A refinery, differential process apparatus, as described in claim 64, and said first refining environment comprises a liquid conduction environment and wherein the second refining ambient comprises a gaseous conduction environment. 73. A differential processing refinery apparatus, as described in claim 66, wherein said first refining environment comprises a liquid conduction environment, wherein said second refining ambient comprises a gaseous conduction environment wherein the third refining environment comprises an ambient of combined, liquid and gaseous driving. 74. A refinery apparatus, of differential process, as described in claim 73, and said heat source to which said sensitive material comprises a heat source which achieves a material temperature of at least about that selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, and in which input dich continuously accepts at least some of the hydrocarbon material heavy, selected from the group consisting of: heavy oils, asphalt, tar, bitumen, material that has an API gravity of less than 11 ° API, material that has an API gravity of less than 10 ° API, material that has a lower API gravity 7th API, material that has a severe API less than 3 ° API, material that has significant amounts of waste, material that has at least 5% by weight of waste, material that has at least 7% weight of waste, material that has at least 10% by weight of waste, and material that has at least 15% by weight of waste. 75. A refinery, differential process apparatus, as described in claim 72, and said refining apparatus has an effective process length and wherein said liquid conduction environment has a length selected from the group consisting of: at least about 1/3 of said process length, and at least about 1/2 of said process length. 76. A differential process refinery apparatus, as described in claim 70, further comprising a high conductive energy transfer element, which is effective in an effective length of the process, and where this effective length of the process is coordinated with a refinery characteristic, selected from the group consisting of the amount of heat transfer in said apparatus, the speed at which the apparatus operates, the amount of heat supplied in said apparatus, the amount of heat transfer in said gaseous conduction environment , the amount of heat transfer in said high conductivity energy transfer element, the kinetics of the coking reactions, occurring within said refinery apparatus, and the permutations and combinations of each of the foregoing. 77. A differential processing refinery apparatus, as described in claim 76, wherein said effective process length comprises at least one length of coke formation. 78. A differential processing refinery apparatus, as described in claim 72 or 76, further comprising a continuous output element of the coke, to which said remaining material is responsive. 79. A differential processing refinery apparatus, as described in claims 72 or 76, further comprising a movement element to which said material containing at least some of the hydrocarbon material is responsive. , 80 A differential processing refinery apparatus, as described in claim 79, wherein said movement element to which said material containing at least some of the heavy hydrocarbon material is responsive, comprises an inclined movement element. 81. A differential processing refinery apparatus, as described in claim 80, wherein said inclined movement element comprises an inclined screw. 82. A differential processing refinery apparatus, as described in claim 79, wherein said moving element, at least one said material containing at least some of the heavy hydrocarbon material is responsive, comprises an element of movement through said liquid driving environment and said gaseous conduction environment. 83. A refinery, differential process apparatus, as described in claims 72 or 76, which further comprises a liquid seal within said refinery apparatus, between said inlet and said outlet. 84. A differential processing refinery apparatus, as described in claim 83, wherein said liquid seal within said process container, between said inlet and said outlet, comprises the heavy hydrocarbon material. 85. A refinery, differential process apparatus, as described in claim 84, and that the seal of the liquid within said process container, between said inlet and said outlet comprises a liquid seal, selected from the group consisting of: a less a seal of approximately 0.07 kg / cm2, at least a seal of approximately 0114 kg / cm2, a seal that has at least 62 cm of liquid column, a seal that has at least 30.5 of liquid column, a seal placed around halfway between an entrance and an exit, or adequate seal to avoid the subsequent blowing of the refined material. 86. A method to refine differentially heavy hydrocarbon materials, this method comprises the steps of: a) entering a material containing at least some heavy hydrocarbon material; b) heating said material; c) initiate the refining of the material in a prime refinery environment; d) continue to refine the material in a second refining environment; e) collect at least some of said refinery products; and f) produce a residue of said material. 87. A method for differentially refining heavy hydrocarbon materials, as described in claim 86, wherein said step of heating the material comprises the step of substantially exceeding the coke formation temperature within said material. 88. A method for differentially refining heavy hydrocarbon materials, as described in claim 86, wherein the step of substantially exceeding the temperature of coke formation within said material comprises the step of achieving at least one temperature selected from the group consisting of : 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, where said input continuously accepts at least some of the hydrocarbon material heavy, selected from the group consisting of: heavy oils, asphalt, bitumen tar, material having an API gravity less than 11 ° API, material having an API gravity less than 10 ° API, material having an API gravity less than 7 API, material having API gravity less than 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material which has at least 10% by weight of waste, and material that has at least 15% by weight of waste. 89. A method for refining differentially heavy hydrocarbon materials, as described in claim 86, further comprising the step of subjecting said material to a third refining environment. 90. A method for refining differentially heavy hydrocarbon materials, as described in claim 89, wherein the step of subjecting said material to a third refining environment comprises step d using a refining environment, which is a combination of said first refining environment and dich second refining environment 91. A method for refining differentially heavy hydrocarbon materials, as described in claim 89, wherein the step of subjecting said material to a third refining environment comprises step d using a transition refining environment, which makes transitions between the first refining environment the second refining environment. 92. A method for refining differentially heavy hydrocarbon materials, as described in claim 91, wherein the step of using a transition refining ambient, which makes transitions between said first refining environment and said second refining ambient, is selected of the group consisting of: a gradual transition environment and a linear transition environment. 93. A method for refining differentially heavy hydrocarbon materials, as described in claim 86, wherein said step of starting the refining of the material in a first refining environment, comprises the step of establishing a first thermal environment, in which the material process and where said stage d continue the refining of the material in a second refining environment comprises the stage of establishing a second thermal environment within which the material is processed. 94. A method for refining differentially heavy hydrocarbon materials, as described in claim 89, wherein the steps of starting the refining of the material in a first refining environment, continuing the refining of the material in a second refining environment, and subjecting said material to a third ambient of refining, each one comprises the stage of establishing different thermal environments. 95. A method for refining differentially heavy hydrocarbon materials, as described in claim 86, wherein the step of initiating the refining of the material in a first refining environment comprises the step of establishing a liquid conduction environment, wherein said step of continuing the refining of the material and a second refining environment comprises stage d establishing a gaseous conduction environment. 96. A method for refining differentially heavy hydrocarbon materials, as described in claim 89, wherein the step of initiating the refining of the material in a first refining environment comprises the step of establishing a liquid driving environment, wherein the step of continuing refining the material in a second refining environment comprises stage d establishing a gaseous conduction environment, and where the step of subjecting said material to a third environment refining comprises the stage of establishing an environment which combines both a liquid conduction environment as a gaseous conduction environment. 97. A method for refining differentially heavy hydrocarbon materials, as described in claim 96, wherein the step of substantially exceeding the coke formation temperature within said material comprises the step of achieving at least one temperature selected from the group consisting of of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, in which said input continuously accepts at least some material from heavy hydrocarbons, selected from the group consisting of: heavy oils, asphalt, bitumen tar, material having an API gravity of less than 11 ° API, material having an API gravity of less than 10 ° API, material having a lower API gravity 7th API, material that has an API gravity of less than 3 ° API, material that has significant amounts of waste, material that has at least 5% by weight of waste, material that has at least 7% by weight of waste, material that has at least 10% by weight of re wastes, and material that has at least 15% by weight of waste. 98. A method for differentially refining heavy hydrocarbon materials, as described in claim 95, wherein the steps of establishing a liquid conduction environment and establishing a gaseous conduction environment, both occur in a process container, which has an effective length of the process and wherein said step of establishing a liquid driving environment comprises the step of establishing a liquid driving environment in a selected location of the group consisting of: about one third of said process container, about half of said process container , approximately the lower third of said process container and approximately the lower half of said process container. 99. A method for differentially refining heavy hydrocarbon materials, as described in claim 93, wherein the steps of establishing a first thermal environment within which the material is processed and establishing a second thermal environment within which the material is processed, both they occur in a process container, which has an effective length of the process and also comprises the step of coordinating said effective length of the process with a refinery characteristic, selected from the group consisting of: the amount of heat transfer in said apparatus, the speed to which said apparatus is operated, the amount of heat supplied in said apparatus, the amount of heat transfer in said gaseous conduction environment, the amount of heat transfer in an energy transfer element, the kinetics of the coking reactions, that occur within said refinery apparatus, and the permutations and combination It is from the previous ones. 100. A method for differentially refining heavy hydrocarbon materials, as described in claim 99, wherein said effective length of the process comprises at least one length of coke formation. 101. A method for refining differentially heavy hydrocarbon materials, as described in claims 95 or 99, further comprising the steps of: a) forming coke of at least some of said material; and b) continuously stirring said coke. 102. A method for refining differentially heavy hydrocarbon materials, as described in claims 95 or 99, further comprising the step of moving said material from an inlet to an outlet. 103. A method for refining differentially heavy hydrocarbon materials, as described in claim 102, wherein the step of moving said material from an inlet to an outlet comprises the step of moving said material upwardly by an inclination between said inlet and said departure. 104. A method for refining differentially heavy hydrocarbon materials, as described in claim 103, wherein the step of moving said material upwardly at an inclination between said inlet and said outlet, comprises the step of boring the material upwardly through the bore. said inclination. 105. A method for refining differentially heavy hydrocarbon materials, as described in claim 102, wherein the step of moving said material from an inlet to an outlet comprises the step of moving said material from said first refining environment said second refining environment . 106. A method for refining differentially heavy hydrocarbon materials, as described in claims 95 or 99, further comprising the step of establishing a liquid seal between an inlet and an outlet. 107. A method for refining differentially heavy hydrocarbon materials, as described in claim 106, wherein said step of establishing a liquid seal, between an inlet and an outlet, comprises the step of using at least some of said heavy hydrocarbon material. . 108. A method for refining differentially heavy hydrocarbon materials, as described in claim 107, wherein said step of establishing a liquid seal, between an inlet and an outlet, comprises the step of establishing a liquid seal, selected from a group that It consists of: at least a stamp of approximately 0.07 kg / cm2, at least a stamp of approximately 0.1 kg / cm, a stamp that has at least 61 cm of liquid d column, a stamp that has at least 30.5 cm of liquid d column , a seal placed approximately in the middle between an entrance and an exit, an adequate seal to avoid the subsequent blowing of the refined material. 109. A refinery apparatus, which comprises: a) an inlet, adapted to accept continuous material, in which said material contains "at least some heavy hydrocarbon material, b) a heat source, to which said responsive material, and which causes volatilized substances to be emitted from said material, c) an inclined area of the refining process, within which at least some of said material and less some of the volatilized substances are contained, d) an element of inclined movement, to which material is responsive, and e) an exit of volatile materials, which is adapted to receive at least some of the volatilized substances. 110. A refinery apparatus, as described in claim 109, wherein said heat source, to which said material is responsive, comprises a heat source that achieves a temperature of the material at least about that selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C 648 ° C, and in which said input continuously accepts at least some of the heavy hydrocarbon material , selected from the group consisting of: heavy oils, asphalt, bitumen tar, material having an API gravity of less than 11 ° API material that has an API gravity of less than 10 ° API material that has an API gravity of less than 7 ° API, material having an API gravity of less than 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material having a less than 10% by weight of waste, and material that has less than 15% in waste weight. 111. A refinery apparatus, as described in claim 109, wherein said inclined refining process area, within which at least some of said material and at least some volatilized substances are contained, has an upper part of the inlet end. and a bottom part of the outlet end, and where said bottom part of the exit end is greater than said upper part of the entrance end. 112. A refinery apparatus, as described in claim 109, wherein said inclined area of the refining process within which at least some of said material and at least some volatilized substances are contained, has a selected group inclination consisting of at least approximately: 15 °, 22.5 ° 30 ° and 45 °. 113. A refinery apparatus, as described in claim 111, wherein said outlet end bottom portion is substantially larger than said upper end entrance part. 114. A refinery apparatus, as described in claim 109, wherein said inclined refining process area comprises an inclined area of seal creation refining process. 115. A refinery apparatus, as described in claim 114, wherein said inclined area of seal creation refining process comprises the input material. * 116. A refinery apparatus, as described in claim 115, wherein said inclined area of seal creation refining process comprises a seal selected from a group consisting of: at least a seal of approximately 0.07 kg / cm2 , at least one seal d approximately 0.14 kg / cm2, a seal that has at least 6 cm of liquid column, a seal that has at least 30 cm of liquid column, a seal located in the middle between an entrance and a outlet, a suitable seal to avoid the subsequent blowing of the refined material. 117. A refinery apparatus, as described in claim 109, in which said inclined movement element, to which said material is responsive, comprises an inclined movement element of excessive power. 118. A refinery apparatus, as described in claims 109, 112, 114 or 116, which further comprises a continuous coke production element, to which said remaining material is responsive. 119. A refinery apparatus, as described in claim 109, further comprising: a) a first refining environment, within which the material is processed; and b) a second refining environment, within which the material is processed. 120. A refinery apparatus, as described in claim 119, wherein the first refining means comprises a liquid conduction environment and wherein the second refining means comprises a gaseous conduction environment. 121. A refinery apparatus, as described in claims 109, 112 or 116, further comprising a liquid seal, within said process container between said inlet and said outlet. 122. A refinery apparatus, as described in claim 121, wherein said liquid seal, within the process container, between said inlet and outlet outlet, comprises a heavy hydrocarbon material. 123. A refinery apparatus, as described in claim 109, further comprising a high conductive energy transfer element d. 124. A refinery apparatus, as described in claim 123, wherein the high-energy energy transfer element comprises an energy transfer element d selected from the group consisting of: a fluidized bed, a transfer element d energy having a conduction value of at least Btu / hr / ft2 / ° F (24,438 Kcal / hr / m2 / ° C), an energy transfer element d, which has a conduction value of at least 20 Btu / hr / ft 2 / ° F (97.75 Kcal / hr / m2 / ° C), or energy transfer element, which has a conduction value of at least 50 Btu / hr / ft 2 / ° C (244.3 (Kcal / hr / m2 / ° C), an energy transfer element that has a conduction value of at least 10 Btu / hr / ft / ° F (488.75 Kcal / hr / m2 / ° C). 125. A refinery apparatus, as described in claim 123, wherein said high conductivity energy transfer element d comprises: a) an area; and b) a gas fed. 126. A method for refining a hydrocarbon material, this method comprises the steps of: a) entering a material containing the least one of the hydrocarbon material; b) heating said material; c) refine said material in an inclination, while refined products are created; and d) producing said refined products. 127. A method for refining a hydrocarbon material, as described in claim 126, and said step of heating said material comprises the step of substantially exceeding the temperature of formation of the coke within said material. 128. A method for refining a hydrocarbon material, as described in claim 127, and said step of substantially exceeding the temperature of formation of the coke within said material, comprises the step of achieving at least about a temperature selected from the group consisting of of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, and in which input dich continuously accepts at least some of the material d heavy hydrocarbons, selected from the group consisting of: heavy oils, asphalt, bitumen tar, material that has an API gravity of less than 11 ° API, material that has an API gravity of less than 10 ° API, material that has a lower API gravity of 7 ° API, material that has a severe API less than 3 ° API, material that has a significant amount of waste, material that has at least 5 weight of waste, material that has at least 7% weight of waste, material that has at least 10% in waste weight, and m material that has at least 15% by weight d waste. 129. A method for refining a hydrocarbon material, as described in claim 126, is that the step of refining said material at an incline, while creating refined products, comprises step d refining said material at an inclination having a top portion. of input and an output background part, - where said output background part is larger than the upper input part. 130. A method to refine a material d The hydrocarbon, as described in claim 126, wherein the step of refining said material at an incline, while creating refined products, comprises the step of refining said material at an inclination having a selected inclination of the group consisting of less about 15 °, a slope of at least about 22.5 °, an inclination of at least about 30 °, and a slope of at least about 45 °. 131. A method for refining a hydrocarbon material, as described in claim 129, is that said material has a liquid level, and where part of the outlet bottom is substantially above the liquid level. 132. A method for refining a hydrocarbon material, as described in claim 126, is that the step of refining said material at a tilt while creating refined products, comprises step d establishing a liquid seal between an inlet and an outlet, through the action of said inclination. 133. A method for refining a hydrocarbon material, as described in claim 132, is that the step of establishing a liquid seal between an inlet and an outlet, through the action of said inclination, comprises the step of using said liquid material. hydrocarbon. 134. A method for refining a hydrocarbon material, as described in claim 133, is that the step of establishing a liquid seal, between an inlet and an outlet, comprises the step of establishing a liquid seal, selected from the group consisting of of: at least a seal of approximately 0.07 kg / cm2, at least a seal of approximately 0.14 kg / cm2, a seal that has at least 61 cm of liquid column, a seal that has at least 30.5 cm of liquid column, a seal located halfway between an entrance and an exit, an adequate seal to avoid the later blowing of the refined products. 135. A method for refining a hydrocarbon material, as described in claim 126, and said step of refining the material at an incline, while creating refined products, comprises the step d moving said material in a manner that exceeds the effects of said inclination. 136. A method for refining a hydrocarbon material, as described in claims 126 130, 132 or 134, further comprising the steps of: a) forming coke from at least some of said material and b) continuously removing said coke. 137. A method for refining a hydrocarbon material, as described in claim 126, includes said step of refining the material on an incline, while creating refined products, comprising the steps of: a) stabilizing a first thermal environment within which the material is processed; and b) stabilize a second thermal environment, within which the material is processed. 138. A method for refining a hydrocarbon material, as described in claim 137, and said step of establishing a first thermal environment within which the material is processed, comprises the stage of establishing a liquid conduction environment, and wherein said step of establishing a second thermal environment within which the material is processed, comprises the stage of establishing a gaseous conduction environment. 139. A method for refining a hydrocarbon material, as described in claims 126 130 or 132, further comprising the step of establishing a liquid seal between an inlet and an outlet. 140. A method for refining a hydrocarbon material, as described in claim 139, is that the step of establishing a liquid seal between an inlet and an outlet comprises the step of using at least some of said hydrocarbon material. 141. A method for refining a hydrocarbon material, as described in claim 126, further comprising the step of driving highly energized into said material. 142. A method for refining a hydrocarbon material, as described in claim 141, is that the step of driving high energy into material comprises the step of using an energy transfer element, selected from the group consisting of a fluidized bed. , a transfer element d energy that has a conduction value of at least Btu / hr / ft2 / ° F (24,438 Kcal / hr / m2 / ° C), an element d energy transfer, which has a conduction value of at least 20 Btu / hr / ft / ° F (91. 15 Kcal / hr / m2 / ° C) or energy transfer element, which has a conduction value of at least 50 Btu / hr / ft2 / ° C ( 244.3 (Kcal / hr / m / ° C) and an energy transfer element that has a conduction value of at least 10 Btu / hr / ft2 / ° F (488.75 Kcal / hr / m2 / ° C). 143. A method for refining a hydrocarbon material, as described in claim 141, is that the step of driving highly energy within said material comprises the step of using a sand bed a gas charge. 144. A refinery apparatus, which comprises: a) an inlet, adapted to accept continuous material, in which said material contains at least some of the heavy hydrocarbon material; b) a source of heat, to which said material is responsive, and which causes volatilized substances to be emitted from said material; c) a refining process area, within which at least some of said material and at least some of said volatilized substances are contained; d) a liquid seal, established at an interface, between said material and said volatilized substances; and e) a volatile outlet, which is adapted to receive at least some of said volatile substances. 145. A refinery apparatus, as described in claim 144, wherein said source of heat to which said material is responsive, comprises a heat source that achieves a temperature of the material at least that selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, and in which said input continuously accepts at least some heavy hydrocarbon material, selected from the group consisting of: heavy oils, asphalt, tar bitumen, material that has an API gravity lower than 11 ° API, material that has an API gravity less than 10 ° API, material that has an API gravity less than 7 ° API , material having an API gravity of less than 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material having at least 10% by weight of waste, and material having at least 15% by weight of r isides 146. A refinery apparatus, as described in claim 144, wherein said liquid seal, established at an interface, between said material and said volatilized substances comprises a heavy hydrocarbon material. 147. A refinery apparatus, as described in claim 146, further comprising a waste outlet, which is adapted to receive at least some waste from said refining process area. 148. A refinery apparatus, as described in claims 144 or 146, wherein said liquid seal comprises a seal selected from the group consisting of: at least one seal of approximately 0.07 kg / cm2, unless a seal of approximately 0.14 kg / cm2, a seal that has at least 61 cm of liquid column, a seal that has at least 30.5 cm of liquid column, a seal located in the middle between an inlet and an outlet, an adequate seal to avoid subsequent blowing Give them refined products. 149. A refinery apparatus according to * is described in claim 148, wherein said source of heat, to which said material is responsive, comprises a heat source which achieves a temperature of the material at least around that selected from the group that It consists of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C 648 ° C, and in which said input continuously accepts at least some of the heavy hydrocarbon material, selected from the group consisting of: heavy oils, asphalt, bitumen tar, material having an API gravity of less than 11 ° API material that has an API gravity of less than 10 ° API material that has a lower API gravity 7th API, material having API gravity less than 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material that has at least 10% by weight of waste, and material that has less than 15% by weight of waste. 150. A refinery apparatus, as described in claim 144, further comprising: a) a sweep gas inlet, established behind said liquid seal; and b) a sweep gas outlet, established behind said liquid seal. 151. A refinery apparatus, as described in claim 144, further comprising a continuous d output element of the coke. 152. A refinery apparatus, as described in claim 146, further comprising: a) a first refining environment, within which the material is processed; and b) a second refining environment, within which the material is processed. 153. A refinery apparatus, as described in claim 152, wherein said first refinery environment comprises a liquid conduction environment wherein said second refinery environment comprises a gaseous conduction environment. 154. A refinery apparatus, as described in claim 144, further comprising a moving element within said refining process area. 155. A refinery apparatus, as described in claim 154, wherein said moving element, within the refining process area, comprises an inclined movement element. 156. A refinery apparatus, as described in claim 155, wherein said inclined movement element comprises an inclined screw. 157. A refinery apparatus, as described in claim 154, wherein said moving element comprises an element of movement through a liquid conduction ambient and a gaseous conduction environment. 158. A refinery apparatus, as described in claim 147, further comprising a moving element, which operates between said inlet and said waste outlet. 159. A method for refining hydrocarbon material, comprising the steps of: a) entering a material containing at least some of the hydrocarbon material; * b) heat said material; c) establish a liquid seal between an entry and an e and d) produce refined products. 160. A method for refining hydrocarbon materials, as described in claim 159, wherein said step of heating said material comprises the step of substantially exceeding the temperature of formation of the coke within said material. 161. A method for refining hydrocarbon materials, as described in claim 160, wherein said step of substantially exceeding the coke formation temperature within said material comprises the step of at least achieving approximately - temperature, selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, * 538 ° C, 593 ° C and 648 ° C, in which said input continuously accepts at least some heavy hydrocarbon material, selected from the grup - consisting of: heavy oils, asphalt, bitumen tar, material having an API gravity of less than 11 ° API, material having an API gravity of less than 10 ° API, material having an API gravity of less than 7 ° API, material having an API gravity of less than 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material having a less 10% by weight of waste, and material having at least 15% by weight of waste. 162. A method for refining hydrocarbon materials, as described in claim 159, wherein said step of establishing a liquid seal between an inlet and an outlet comprises the step of using at least some of said hydrocarbon material. 163. A method for refining hydrocarbon materials, as described in claim 162, further comprising the step of producing waste. 164. A method for refining hydrocarbon materials, as described in claims 159 or 162, wherein said step of establishing a liquid seal, between an inlet and an outlet, comprises the step of establishing a liquid seal, selected from the group consisting of of: at least one seal of approximately 0.07 kg / cm2, at least one seal of approximately 0.14 kg / cm2, a seal having at least 61 cm of liquid column, a seal having at least 30.5 cm of liquid column, a seal located in the middle between an inlet and an outlet, an adequate seal to avoid the subsequent blowing of the refined products that result from said step of continuously volatilizing the substances. 165. A method for refining hydrocarbon materials, as described in claim 164, and said step of heating the material comprises the step of achieving at least about a temperature selected from the group consisting of: 343 ° C, 371 ° C, 399 ° C, 426 ° C, 481 ° C, 510 ° C, 538 ° C, 593 ° C and 648 ° C, and in which input dich continuously accepts at least some of the heavy hydrocarbon material, selected from the group consisting of: petroleum heavy, asphalt, bitumen tar, material that has an API gravity of less than 11 ° API, material that has an API gravity of less than 10 ° API, material that has an API gravity of less than 7 ° API, material that has a lower severe API of 3 ° API, material having significant amounts of waste, material having at least 5% by weight of waste, material having at least 7% by weight of waste, material having at least 10% by weight of waste, and material that has at least 15% by weight of waste. 166. A method for refining hydrocarbon materials, as described in claim 159, further comprising the steps of: a) entering a scavenging gas above said liquid seal; and b) releasing said sweeping gas above said liquid seal. 167. A method for refining hydrocarbon materials, as described in claim 159, further comprising the steps of: a) forming coke from at least some of said material; and b) continuously stirring said coke. 168. A method for refining hydrocarbon materials, as described in claim 159, wherein said step of heating the material, comprises the steps of: a) establishing a first thermal environment, within which the material is processed; b) establish a second thermal environment, within which the material is processed. 169. A method for refining hydrocarbon materials, as described in claim 168, and that the step of establishing a first thermal environment within which the material is processed, comprises stage d establishing a liquid conduction environment, and where dich stage of establishing a second thermal environment, within which the material is processed, comprises stage d establishing a gaseous conduction environment. 170. A method for refining hydrocarbon materials, as described in claim 159, further comprising the step of moving said material from an inlet to an outlet. 171. A method for refining hydrocarbon materials, as described in claim 170, wherein said step of moving the material from an inlet to an outlet, comprises the step of moving said material upwardly in an inclination between said inlet and said outlet. 172. A method for refining hydrocarbon materials, as described in claim 171, wherein said step of moving the material upwardly in an inclination between said inlet and said outlet comprises the step of "drilling said material upwards of the inclination. 173. A method for refining hydrocarbon materials, as described in claim 170, wherein said step of moving the material from an inlet to an outlet, comprises the step of moving said material from a first refining environment into a process container, to a second refining environment, inside said process container.