WO2025184735A1 - Pyrolysis device, short path cracking process and reactor, for cracking organic feed materials to produce liquid fuel and/or hydrocarbon products, material, methods for manufacturing the equipment, using the equipment and uses of the products thereby produced - Google Patents

Abstract

The present invention relates to a short-path pyrolysis system for selective product recovery and rapid solid elimination. It enables efficient thermal decomposition of variable feed materials, including hydrocarbons, biomass, plastics, and tires. The system features high-temperature filters for micro-solid removal and self-cleaning condensers to reduce fouling while maximizing yield and selectivity. It includes a reaction surface, heating means, spray nozzles, vapor and solids exit, and reflux condensation for controlled separation in an oxygen-depleted or inert gas environment. The invention also covers equipment manufacturing and adaptive process management for continuous optimization, making it ideal for waste valorization and sustainable products and fuel production.

Description

PYROLYSIS DEVICE, SHORT PATH CRACKING PROCESS AND REACTOR, FOR CRACKING ORGANIC FEED MATERIALS TO PRODUCE LIQUID FUEL AND/OR HYDROCARBON PRODUCTS, MATERIAL, METHODS FOR MANUFACTURING THE EQUIPMENT, USING THE EQUIPMENT AND USES OF THE PRODUCTS THEREBY PRODUCED

FIELD OF THE INVENTION

[0001] The present invention relates to a short-path pyrolysis system for selective product recovery and rapid solid elimination. It enables efficient thermal decomposition of variable feed materials, including hydrocarbons, biomass, plastics, and tires. The system features high- temperature filters for micro-solid removal and self-cleaning condensers to reduce fouling while maximizing yield and selectivity. It includes a reaction surface, heating means, spray nozzles, vapor and solids exit, and reflux condensation for controlled separation in an oxygen-depleted or inert gas environment. The invention also covers equipment manufacturing and adaptive process management for continuous optimization, making it ideal for waste valorization and sustainable products and fuel production.

BACKGROUND OF THE INVENTION

[0002] When submitting oils or other hydrocarbons to thermal cracking in an indirectly fired rotating kiln, there are several major problems. The bigger ones are the production of solids and/or some of the products of the pyrolysis foul downstream equipment like pipes, condensers, fractionation equipment etc.

[0003] One such problem is keeping the coke, formed in the cracking reactions, from coating the reactor walls and internals, thus impeding heat transfer from the heat source to the inside of the kiln. Often charges of sand or metal are added to the kiln to scrape the walls of the kiln as it rotates. Coke rarely deposits in a uniform layer. An uneven coke layer can result in hot spots and eventual failure of the reaction surface support.

[0004] A second problem is the entrainment of coke or long molecules that increase potential fouling and reduce the quality of the products. This is a major problem when there is a liquid mass (ex: hot liquified plastics, hot oil etc.) over the reaction surface (reaction area).

[0005] A third problem is the formation of long molecules and molecules with high melting points or sublimation points (Waxes and some aromatics). These will increase the fouling of downstream pipes and equipment. This is especially important when the feedstock comprises different plastics or organic materials.

[0006] The fourth problem is getting the required heat from its source to the reaction site. Typically, in a kiln, the heat transfer area in contact with the reactants is a small portion on the kiln shell. Further, charges added to the kiln without being previously heated outside of the kiln will form a resistance to heat transfer.

[0007] In thermal cracking, the reaction temperature (and pressure) must be kept in a narrow operating range to increase the yield of the desired product slate. If the temperature at the reaction site is too cold, the reaction will take longer and the feed rate will have to be reduced. If the temperature is too high, product quality and quantities are compromised. Therefore, for a given feedstock, reactor size and pressure, the temperature at the reaction site must be closely measured and controlled. This is difficult when the reactor wall cokes up or when the metal charge has trapped the coke within when measuring the temperature on the outside of the reactor shell but the reaction is inside the reactor shell.

[0008] Finally, once the coke has been released, either when the reaction takes place or after it has been scraped off the surface it was attached to (i.e. on the charge or on the reactor walls), the coke must exit the reactor without plugging the exit from the reactor thereby causing pressure surges and failure of the reactor seals, often resulting in fires.

[0009] Rotating kilns, both directly fired (heat source or flame(s) inside the kiln) and indirectly fired (heat source or flame outside the kiln) have been used in various applications for more than 100 years. When hydrocarbons are being treated in a rotating kiln to make a specific slate of oil products, plastics and organic materials an indirectly fired kiln is often used.

[0010] One of the earliest applications for indirectly fired kilns was the production of coal oil and gas by thermal cracking and vaporization of coal.

[0011] At present, no fully satisfying solution has been identified in response to the numerous technical difficulties encountered by the following prior equipment and/or processes.

[0012] Holighaus et al. (CA 1 221 047) mentions that to avoid coke deposits building up on the inside of the walls of the drum, the latter contained steel balls that remove deposits from the walls by attrition as the drum revolved. The kiln is slanted toward the exit end, where a stationary box is located. A screen, attached to the kiln, keeps the metal charge in the kiln. The box has two exits, one for the hydrocarbon vapours at the top and a pipe at the bottom of the box for the solids. [0013] Bernt (CA 1 129 195) suggests that chains, attached to spoons, are effective in removing coke deposits from the walls of a rotating kiln.

[0014] Musha and Maeda (US 4 014 643) describe a similar apparatus with chains attached to lifters to break down the coke on the kiln walls as the kiln rotates.

[0015] Klaus (CA 1 334 129) mentions that the solid pyrolyzed coke is removed from the reactor walls by the grinding bodies and the resulting small particles are directed to the centre of the kiln with spiral fins and continuously removed from the reactor through ports in the reactor walls. The ports open into a stationary ring around the kiln. Vapours exit through the top of the ring, while the fine solids exit through the bottom of the ring. Screens keep the grinding bodies in the kiln.

[0016] Taciuk et al. (CA 2, 186,658) describes a charge of ceramic halls or coarse granular solids provided within the vessel chamber. As the vessel rotates, the ceramic balls or the granular solids scour the vessel’s internal surface and comminute the coke into fine solids. The coke is directed to one end of the kiln with spiral fins continuously welded to the reactor wall. A spiral chute with a screen at its entrance transports the coke up to the exit pipe. The exit pipe, at the centre of the exit end of the kiln, has a screw conveyor to take the coke out of the reactor. These beds of solids constitute a resistance to heat transfer, especially when coke is captive in the interstices between the solids forming the charge.

[0017] Indirectly fired rotating kilns are not very efficient in transferring heat to the hydrocarbons to be cracked and/or vaporized through the shell. Some use a stream of solids circulating between two kilns: The process kiln, where the solids release the heat they contain to the hydrocarbon to be treated, and another kiln where the coke that deposited on the solids is burned off, heating the solids, which are then returned to the first kiln.

[0018] Taciuk et al., CA 1 120 418, suggest the use of a stream of sand to carry heat from an outer kiln, where the burner is situated, to the inner kiln, where the tar sands is vaporized and/or thermally cracked.

[0019] Raymond and McKenny, CA 2 151 792, suggest the use of a stream of ceramic or Pyrex® glass balls circulating between an indirectly fired rotating kiln where a coal and oil mixture are pyrolyzed, and a directly fired kiln where the coke is burned off the balls, cleaning and heating them. The hot balls are then returned to the first kiln, where they release some of the heat required for the process.

[0020] In a similar process, Taylor, US 5 423 891 mentions a heat-carrying solid (HCS) such as iron oxide, aluminium oxide, refractory inert, fine mesh sand, or retorted residue from the starting waste material, circulating between a dryer, where the coke is burned off and the HCS is heated, and the thermal cracking kiln where the “gasification” of solid waste material takes place.

[0021] These prior art processes involve significant material handling difficulties encountered in the conveyance of large amounts of hot solids.

[0022] Others suggest using fins attached to the kiln walls to enhance heat transfer from the heat source through the reactor walls.

[0023] Peterson and Wilson, (CA 1 316 344), describe a plurality of fins extending from the inner wall and transmitting heat from the inner wall to the particulate material.

[0024] Kram et al. (US 4 131 418) mention heat exchange fins on the inside of cooling tubes to enhance the cooling of solids particulates.

[0025] Hogan (US 4 872 954) mentions fins affixed to the exterior surface of the drum of a retort for treating waste.

[0026] Fins continuously welded to the wall of a kiln can cause stress and failure of the kiln wall due to the differential expansions of the wall and of the fins. Also, fins inside the kilns are surfaces that are easily covered in coke, causing hot and cool spots; furthermore, they are difficult to clean. Lifters and mixers in rotating kilns are mentioned in several patents, usually to enhance the mixing of material within a directly fired kiln (i.e. the flame is inside the kiln along with the material to be dried, burned, incinerated, calcined and/or decoked).

[0027] Tyler (US 4 47 ,886), Leca (GB 1 534 302), Ellis (GB 2 150 271), Schoof (WO 1997/046843), Hojou (JP2007 040615), Omiya (JP 2006 0309565) and Doeksen (CA 2315774) all describe lifters or mixers, attached to the kiln wall and protruding through the ceramic lining of a directly fired kiln. Vering (US 3 807 936) describes blade lifters to be used in kilns treating abrasive materials such as cement clinkers.

[0028] Twyman (CA 1 099 507) mentions curved lifters, attached to the kiln wall, as mixing paddles in a directly heated kiln with flue gas as the source of heat. In a similar kiln, Musha et al. (US 4014643) mentions attaching chains and spoons to the end of each mixing paddle to scrape the kiln walls and the lifter below clean of coke or other deposits in kilns used as dryers for slurries before they are fed to incinerators.

[0029] All these mixers and lifters are suggested as means to turn over the material to be treated and show more of the untreated material to the source of heat. [0030] Wheeler et Al. in CA 2 799 751 describes a reactor and its internals used for the thermal processing of a liquid mixture. The reactor comprises plates, and at least part of the surface of said plates is used to perform the thermal processing. The reactor and its internals are used for the thermal processing of various liquid mixtures containing organic compounds. The processes, for thermal processing the mixture comprising organic compounds, comprising the steps of feeding the reactor and its internals and being useful for treating wastes oils and/or for destroying hazardous and/or toxic products; and/or for reusing waste products in an environmentally acceptable form and/or way, and/or for cleaning contaminated soils or beaches, and/or cleaning tar pits, and/or use in coal-oil co-processing, and/or recovering oil from oil spills, and/or PCB free transformer oils. A process for fabricating the reactor and its internals is also proposed.

[0031] US 4 411 074 relates to a process and apparatus for drying oil well cuttings. More particularly, the present invention relates to the direct thermal treatment of oil well drill cuttings whereby the cuttings will be freed from any excess liquid and removed for storage or disposal onsite or bagging.

[0032] US 2009 114567 describes a continuous process and apparatus for treating feedstocks containing carbonaceous materials involves heating bodies to heat the feedstock to vaporize and crack hydrocarbons and carbon formed on heating bodies is removed through direct contact to a flame heater.

[0033] Bertrand (CA 3 005 593) mentions a compact equipment, for performing pyrolysis of a feed material comprising an enclosure at least one reaction’s support preferably positioned inside the enclosure and for performing pyrolysis on at least part of the surface of the reaction’s support, the reaction surface having at least a partially conic shape and being static or rotating.

[0034] Depending on the feed, the above systems have a wide product slate, some coke gets entrained with the product vapors, and the cracked products will foul the downstream equipment with certain feeds.

[0035] There was therefore a need for a process and reactors allowing the thermal processing of various mixtures but free of at least one of the drawbacks of prior art known reactors and/or processes, and preferably all of them.

[0036] There was also a need for reactors and systems that could provide better reaction control of the resulting product slate from various oils, plastics and organic mixtures. There was a need to efficiently eliminate the solids and to eliminate microsolids. There was also a need for a process allowing the treatment of oil mixtures, plastics or mixed organic material with little fouling of equipment downstream of the reactor.

[0037] There was a further need for improving the yield of valuable products and/or by-products in an environmentally acceptable way. There was also a need for new uses for products recovered by thermal treatment.

SUMMARY

[0038] The invention relates to a device for pyrolyzing feed materials to produce valuable products. It comprises an enclosure housing at least one reaction support with a partially conical reaction surface, which may be static or rotating. At the bottom is a solid exit to efficiently take out solids. Positioned above the reaction surface are high-temperature vapor/solid separation devices.

[0039] The system often integrates self-cleaning condensers at the start of the condensation/fractionation phase and/or within the reactor, minimizing fouling and enhancing product recovery. The invention also describes a process for converting hydrocarbon and organic feedstocks — such as heavy oils, plastics, and biomass — into liquid fuels and specialty products. The resulting fuels can be used in various applications, and the invention includes the manufacturing of equipment to support the process.

BRIEF DESCRIPTION OF THE DRAWINGS

[0040] FIG.1 : is a Block flow diagram representing a summary of an embodiment of the process of the present invention

[0041] FIG.1A: is a Block flow diagram representing a summary of an embodiment of the process of the present invention with an optional reflux condenser inside the reactor

[0042] FIG.2: is an overview of the device with a view inside of key elements of the device in particular the colder surfaces and rotating cone but without the insulation.

[0043] FIG.3: is a cross-sectional front perspective view of the reactor equipment device showing the various parts of the reactor and an example of the first heavy hydrocarbon condenser to separate the heavier hydrocarbon products. This is an example of the cone being at 60 degrees down from the horizontal. [0044] FIG.3A: is a cross-sectional front perspective view of the device showing the various parts of the equipment which includes an optional reflux-condenser. This is an example of the cone being at 45 degrees down from the horizontal.

[0045] FIG.4: is a cross-sectional top view (A-A’) (see FIG.3) looking from the top of the enclosed self-cleaning condenser, showing an example of the rotating brushes. The coolant is brought into the plates to keep them at the desired temperature range.

[0046] FIG.4A: is a cross-sectional top view (A-A) (see FIG.3A) looking from the top of the reactor enclosure, showing an example of the optional enclosed reflux-condenser system. The coolant is brought into the plates to keep them at the desired temperature range.

[0047] FIG.5 is a cross-sectional top view (B-B’) (see FIG.3A) of the device, showing an example of the conic reaction surface with two types of scrappers and spray nozzles.

[0048] FIG.6: is a cross-sectional view the same as FIG.3A with the addition of a cyclone, instead of a filter, in the reactor to take out any solids that might be entrained by the vapors. It also includes an optional heating system to reheat the vapors and/or heat the cyclone.

[0049] FIG.7: Is a cross-sectional view the same as FIG.3A but with the angle of the cone being at 60 down from horizontal instead of 45 degrees.

[0050] FIG.8: is a cross-sectional view similar to FIG.7 showing the system with 2 heating cones. It includes using the walls to condense some of the products and return them to the lower reaction surface.

[0051] FIG.9: is a horizontal cross-sectional view (C-C’) of the compact equipment represented on FIG.8 over the topmost reaction surface.

[0052] FIG.10: is a cross-sectional view similar to FIG.7 with the rotating brushes to scrape the cooler plates (condenser elements) out any solid and/or heavy liquid that might stick to them.

BRIEF DESCRIPTION OF THE INVENTION

Preliminary definitions:

[0053] Municipal solid waste (MSW), commonly known as trash or garbage in the United States and as refuse or rubbish in Britain, is a waste type consisting of everyday items that are discarded by the public. Waste can be classified in several ways but the following list represents a typical classification: - biodegradable waste: food and kitchen waste, green waste, paper (most can be recycled although some difficult to compost plant material may be excluded);

- recyclable materials: paper, cardboard, glass, bottles, jars, tin cans, aluminum cans, aluminum foil, metals, certain plastics, fabrics, clothes, tires, batteries, etc.;

- inert waste: construction and demolition waste, dirt, rocks, debris, ;

- electrical and electronic waste (WEEE) - electrical appliances, light bulbs, washing machines, TVs, computers, screens, mobile phones, alarm clocks, watches, etc.;

- composite wastes: waste clothing, Tetra Packs, waste plastics such as toys;

- hazardous waste including most paints, chemicals, tires, batteries, light bulbs, electrical appliances, fluorescent lamps, aerosol spray cans, and fertilizers; and

- toxic waste including pesticides, herbicides, and fungicides.

[0054] Organic material', means organic matter, organic material, or natural organic matter (NOM) refers to the large pool of carbon-based compounds found within natural and engineered, terrestrial and aguatic environments. It is matter composed of organic compounds that has come from the remains of organisms such as plants and animals and their waste products in the environment. Organic molecules can also be made by chemical reactions that don't involve life. Basic structures are created from cellulose, tannin, cutin, and lignin, along with other various proteins, lipids, and carbohydrates. Organic matter is very important in the movement of nutrients in the environment and plays a role in water retention on the surface of the planet. Organic material may also include hydrocarbons and/or MSW or a mixture of the two.

[0055] Contaminants: In MSW, the contaminants are non-combustible material and/or non- organic material, for example metals, stones and glass.

[0056] Liquid fuel: are combustible or energy-generating molecules that can be harnessed to create mechanical energy, usually producing kinetic energy; they also must take the shape of their container. It is the fumes of liguid fuels that are flammable instead of the fluid. Most liguid fuels in widespread use are derived from fossil fuels; however, there are several types, such as hydrogen fuel (for automotive uses), ethanol, and biodiesel, which are also categorized as a liguid fuel. Many liguid fuels play a primary role in transportation and the economy. Liguid fuels are contrasted with solid fuels and gaseous fuels.

[0057] Particulates: many small units of matter of less than 5mm average size when talking of solids. [0058] Vapor/solid separation device: any equipment that separate vapors from solids ex: cyclones, filters, electrostatic precipitators.

[0059] Cleaning device : it is a device that can clean a surface example brushes, scrappers, ultrasonic, gas jets.

[0060] Pellets: means a small rounded compressed mass of substance, that may, for example, be in the general form of spheres, cube and/or cylinders.

[0061] Used Lubricating Oil (ULO): are oils or greases that were used as lubricants, usually in engines, and were discarded. Examples would include car engine oils, compressor oils, and diesel engine oils among others. Lubricating oils generally contain additives, which are carefully engineered molecules added to base oils to improve one or more characteristic of the lubricating oil for a particular use. Used lubricating oil is classified as a hazardous product in many jurisdictions because of its additives and contaminants.

[0062] Organic vapour: is the vapour produced from the pyrolysis of the feed material entering the rotating kiln. The components of the organic vapour may include hydrocarbons and may also comprise of only hydrocarbons.

[0063] Bio-oil: is the product from the condensation of the organic vapour. Bio-oil also includes specific chemicals obtained from the condensed organic vapour, which may be separated eindividually from the other components of the condensed organic vapour.

[0064] Liquification: means to increase the liquid fraction of a material which has at least a solid fraction. The resulting material after liquification is then considered a liquid and may or may not have entrained solids and/or gasses.

[0065] Substantially non-reactive gas. is a gas such as nitrogen, recycled reaction gas, carbon dioxide or water steam that does not affect or enter into the thermal processing or that does not substantially combine with either the feed or reaction products in the reactor operating range, for example in a temperature range ranging from 300 to 850 degrees Celsius, in a temperature range up to 700 degrees Celsius, preferably up to 525 degrees Celsius.

[0066] l/l/aste oils: are oils or greases that are discarded. They include used lubricating oils (ULO) as well as a wide range of other oils such as marpol, refinery tank bottoms, form oils, metal working oils, synthetic oils and PCB-free transmission oils, to name a few.

[0067] Thermal processing/thermally treating: is preferably any change in phase and/or composition, and/or reactions initiated or facilitated by the application, or withdrawal, of heat and/or temperature. Examples of thermal processing include evaporating, cracking, condensing, solidifying, drying, pyrolyzing and thermocleaning. In the meaning of the invention the expressions Thermal processing/thermally treating preferably exclude combustion.

[0068] Sweep gas. is any non-reactive or substantially non-reactive gas. Preferably it is an inert gas such nitrogen, recycled reactor non-condensable gas or water steam. It was surprisingly found that such gas not only have as sweeping effect in the reaction zone of rotating operating reactor, but may help control the pressure in the reactor, may increase the safety in plant operations, may help control the reactions in the reactor and globally may improve the efficiency of the process. For example, the sweep gas is a gas stream that may additionally serve in various the following functions such as:

- when injected into the reactor feed line, the sweep gas changes the density of the total feed stream; it changes the flow regimes within the feed line and/or nozzles, which results in lower incidence of fouling and plugging of the piping and spray nozzles, and in improved spray patterns; further, the sweep gas favours atomization of the organic liquid feed stream before the organic liquid reaches the reaction sites on the hot plates, and/or

- if introduced into the liquid feed at temperatures above that of the organic liquid feed stream, it will increase the feed stream temperature and reduce the energy, or heat, provided by the kiln, and/or

- it reduces the organic vapour’s and/or organic liquid's residence time in the reactor, by sweeping the organic vapours out of the reactor soon after they are formed, thereby reducing the incidence of secondary reactions, or over-cracking, resulting in higher liquid yields and more stable liquid product bio-oils, and/or

- the sweep gas present in the reactor reduces the organic vapour's partial pressure, and favours the vaporization of the lighter organic fractions, for example gasoil and naphtha, in the feed and products; this also reduces over cracking in the lighter fraction and increases the stability of the bio-oil liquid products, and/or

- the sweep gas helps to stabilize the pressure in the reactor, and/or

- when steam or nitrogen are used, the sweep gas reduces the risk of fires in the event of a leak in the reactor or in the downstream equipment; it will disperse the combustible vapours escaping and, hopefully, keep the combustible vapours from igniting, even if they are above their auto-ignition point, and/or

- it can also be part of the stripping gas stream in the product distillation unit.

VARIOUS EMBODIMENTS OF THE INVENTION [0069] Following references and numbers are thereafter identified to identify various components of the process that includes the reactor (short path cracker) represented schematically on FIGs.1,1A, 2, 3, 3A,4, 4A, 5, 6, 7, 8, 9 and 10. In FIG.8 the elements related to the upper reaction surface are shown with an apostrophe (ex: 6’):

[0070] The following is an example of the system where a version of the short path cracker is shown in the third stage of the description. This is an example and does not represent all of the versions of the invention.

[0071] The first stage, the optional pre-treatment, can involve many types of operations on the feedstocks (mixed waste plastic and/or biomass and/or waste oils):

1 . The starting material are broken into small pieces below 20 mm.

2. Metals, glass, dirt, sand and rocks etc. are eliminated as much as possible, preferably by gravity and/or by magnetic separation; Any solids left should be less than 5 mm in diameter.

3. the solid content has been further increased, in a screw press, up to 50 to 60 % and eventually, with special system, such as separation mill, turbo dryer, high efficiency dryer, press, raised up to 85%; and/or

4. a maximum of dewatering can be done by many means: organic solids are increased by mechanical device like a dry Hammermill, a press, screw press or other drying systems like a turbo dryer, high-efficiency dryer, drum and belt dryers and other means to eliminate the water from the feedstock etc. [0072] In the second stage the feedstock exiting the first stage is heated and/or liquified, for example in an extruder. Depending on the feedstocks the temperature needed to liquefy and bring to a temperature near but below the average temperature for cracking the feedstocks. For example for heavy oils like vacuum tower bottoms the temperature can be between 200 to 280 degrees Celsius. For polyethylene plastics, the temperature could be 400° Celsius or slightly more. An inert gas (ex: nitrogen) preferably heated close to the temperature of the feedstock is preferably added at a pressure between the 0.5 and 50 bar. It helps with spraying in the reactor (Short path cracker). See FIG.3 item 8 Exceptionally there is no added gas if in the extruder or heating system if a small part of the feedstock transforms into a vapor and/or gas and drives the pressure necessary for the desired spray pattern from spray nozzles in the reactor.

Third Stage: Short Path Cracker Reactor

[0073] The liquefied feedstock from the second stage enters the reactor, which may be conical (60° angle) and insulated (2, 3, 19, 19') as shown in FIGs.3, 4, and 5. The reactor or short path cracker performs the following steps:

1. Spraying onto Heated Surfaces

The feedstock and optional inert gas mixture enters through pipes (8) and is sprayed via nozzles (9) as fine droplets (21) onto heated conical surfaces (20). These surfaces can be heated by induction coils or similar methods (12) to a temperature of 300°C-800 °C, depending on feedstock. For polyethylene, the surface temperature is preferably 500°C -525 °C.

2. Cracking and Vapor Formation

The droplets absorb heat upon contact with the conical surface (20), causing cracking and/or vaporization. Vapors (and any off-gases) move upward, while solids or coke (13) slide down by gravity into the solids exit (E). If solids adhere to the surface, they are dislodged by scrapers (10) or brushes (23).

3. Scraper Mechanism

The conical surface (20) can rotate, while the scraper (10) remains fixed in contact. Shelves (11) support the rotating surface, driven by a motor (15) and gear (18). The assembly is sealed from outside air at points (14) and (16). If solids are difficult to remove, a rotating brush (23) may be employed. Solids that might otherwise be carried upward by vapors drop out because of the reactor’s vertical orientation and low vapor velocity, and any remaining particulates are captured by a filter (33) before vapor exit (V). 4. Vapor Exit

The vapors exit through a filter to remove microscopic solids and then flow out the vapor exit (V).

Fourth Stage: Primary Condensation

[0074] Vapors from mixed plastics (e.g., PET, PP, LDPE, HDPE) leaving the reactor at exit (V) enter a self-cleaning condenser (34). Cooling plates condense heavier components (e.g., heavier paraffins and terephthalic acid), which flow or are brushed down (6, 36) to the condenser bottom (37) before being drawn off through the product exit (37). A screw conveyor is included because terephthalic acid remains solid at high temperatures (around 300 °C).

Fifth Stage: Final Separation

[0075] The partially condensed vapors, typically around 270 °C at exit (35), can then be directed to additional condensers or a distillation column to separate kerosene, diesel, naphtha, and gases. Because these vapors contain minimal solid particles or fouling contaminants, standard separation techniques can be used effectively. When working with feedstocks containing polyethylene terephthalate (PET), it may be desirable to subject the diesel fraction to a secondary separation step to remove remaining terephthalic acid or other by-products.

[0076] In a different configuration, if the objective is to produce mostly lighter hydrocarbon products such as Naphtha or kerosene and diesel, the reactor is modified to include a reflux condenser (FIG.3A, FIG.4A). The process is the same for the first 2 phases.

Third Stage: Short Path Cracker Reactor

[0077] The liquefied feedstock from the second stage enters the reactor, which may be conical (60° angle) and insulated (2, 3, 19, 19') as shown in FIG.3A, 4A. The reactor or short path cracker performs the following steps:

1. Spraying onto Heated Surfaces

The feedstock and inert gas mixture enters through pipes (8) and is sprayed via nozzles (9) as fine droplets (21) onto heated conical surfaces (20). These surfaces can be heated by induction coils or similar methods (12) to a temperature of 300-800 °C, depending on feedstock. For polyethylene, the surface temperature is preferably 500- 525 °C. 2. Cracking and Vapor Formation

The droplets absorb heat upon contact with the conical surface (20), causing cracking and/or vaporization. Vapors (and any off-gases) move upward, while solids or coke (13) slide down by gravity into the solids exit (E). If solids adhere to the surface, they are dislodged by scrapers (10) or brushes.

3. Heavier Hydrocarbon condensed and cracked

The heavier hydrocarbons in contact with the condenser form droplets (7) or fine solids. They fall back down onto the hot plate where the material is cracked again and the vapors flow up. In many cases, a cleaning system will be added to ensure the cold surfaces are clean and any droplets or particulates are pushed down onto the hot surface (figurelO).

4. Scraper Mechanism

The conical surface (20) can rotate, while the scraper (10) remains fixed in contact. Shelves (11) support the rotating surface, driven by a motor (15) and gear (18). The assembly is sealed from outside air at points (14) and (16). If solids are difficult to remove, a rotating brush (23) may be employed. Solids that might otherwise be carried upward by vapors drop out because of the reactor’s vertical orientation and low vapor velocity, and any remaining particulates are captured by a filter (33) before vapor exit (V).

5. Vapor Exit

The vapors exit through a filter to remove microscopic solids and then flow out the vapor exit (V).

[0078] The fourth and fifth stages are the same except a self-cleaning condenser might not be required.

[0079] FIG.6 is the same as FIG.3A except the filter has been replaced by a cyclone for the vapor/solid separation. Infrared heaters are there to ensure the vapors are far from their dew point when it the cyclone.

[0080] The present application also provides an equipment, short path cracker, for performing pyrolysis and select product (that is preferably of the flash type pyrolysis) and of a feed material, preferably selected in the group constituted by oily feeds, plastics and/or by hydrocarbon feeds and/or by an organic material in the form of agglomerates, and for recovering a fuel (that is preferably a biodiesel or a diesel) or a product, said equipment comprising: o an enclosure having a lateral part substantially vertical, a bottom part and a superior part, said enclosure comprising at least: o feeding means, preferably of the feeding line type with spray nozzles, positioned in the lateral and/or in the bottom part and/or in the upper part of the enclosure, for spraying the feed material that is preferably mainly liquid or in the form of particulates, preferably having a maximum average size of 5 mm; o a vapor exit positioned preferably in the superior part of the enclosure and for evacuating vapors generated during the pyrolysis and/or added steam and/or added inert gas; o a solid exit positioned preferably in the bottom part of the enclosure and for evacuating solids produced during pyrolysis, o at least one reaction’s support preferably positioned inside the enclosure and for performing pyrolysis on at least part of the surface of the reaction’s support, said reaction surface having at least partially a conic shape, the edge of a conic shape being preferably at the top or at the bottom of the conic shape, o direct and/or indirect cleaning means, preferably a scraping device, being positioned inside the enclosure and preferably configured to be in contact with at least part of the surface of the reaction’s support wherein feed material is sprayed and wherein the pyrolysis reaction take place, for cleaning at least part of the surface of the reaction’s support after the pyrolysis reaction has been taking place, and o internal and/or external heating means configured for heating at least part of the reaction support and /or without inducing overheating of the reaction surface o Colder surfaces and/or reflux condenser to condense products with higher melting or sublimation points and return them to the reaction surface and/or take them out of the process

- wherein the reaction’s support and the heating means are preferably closely positioned;

- wherein a relative movement is initiated between cleaning means and the reaction’s support: and

- wherein the reaction’s support is stationary and the cleaning means are moving relatively to the reaction support that is stationary; and/or

- wherein the reaction’s support is moving and the scraping device is stationary; or

- wherein the reaction support and the cleaning means are moving according to identical or different speeds and/or according to identical or different rotation directions and/or according to different and/ or according to parallel trajectories, and -wherein said compact equipment is optionally configured in order the pyrolysis being performed in the enclosure with an atmosphere containing at least one inert gas and/or in atmosphere with a low oxygen content.

[0081] In some embodiments, during operation the colder or reflux condenser surfaces are at least 10 degrees colder than the reaction surfaces. In some embodiments, during operation the cooling surfaces will be between 5 and 280 degrees Celsius.

[0082] In some embodiments, to clean the surfaces or for certain operations, the cooling medium is taken out from the colder surfaces and the temperature left to go up to 750 degrees Celsius.

[0083] In some embodiments, in the case of making diesel or biodiesel and other products the cooling surfaces total sizes is calculated to be able to function at a temperature between 85 and 150 degrees Celsius, preferably around 110 to 130 and more preferably at 120 degrees Celsius while bringing the exiting vapors from the enclosure at between 250 and 310 and more preferably 270 degrees Celsius.

[0084] In some embodiments, the cooling surfaces are cooled by thermal fluid and/or gas.

[0085] In some embodiments, the short path cracker further comprises brushes that can clean the surface of any solid or high viscous condensate material

[0086] In some embodiments, the reaction support is made of a plurality of at least partially conic surfaces.

[0087] In some embodiments, the speed of the reaction’s support relative to the static scraping device ranges from 6 to 60 rpm.

[0088] In some embodiments, the speed of the reaction’s support relative to the static scraping device ranges is about 20 rpm.

[0089] In some embodiments, the axis of the conic reaction surfaces is positioned substantially centrally in the enclosure.

[0090] In some embodiments, the scrapping device comprises scrapping element(s) and is configured in order with scrapping element(s) being in contact of the reaction surfaces when in need to be cleaned, said scrapping element(s) being preferably made of a plurality of scraping items.

[0091] In some embodiments, the scrapping items being a plurality of brushes and/or of blades. [0092] In some embodiments, the scrapping items being preferably positioned substantially symmetrically inside the enclosure.

[0093] In some embodiments, the enclosure has a cylindrical body, a quadratic body or a triangular body and has a top part having preferably a conic form or a pyramidal form with the edge of the form being at the edge of the enclosure and with the bottom part of the enclosure having preferably a conic form or a pyramidal form.

[0094] In some embodiments, the enclosure has a square central body and a top part having preferably a pyramidal form and with the bottom part having preferably a pyramidal form.

[0095] In some embodiments, the short path cracker is configured for performing flash pyrolysis of the feed material, on the surface of the reaction’s support heated to 300 -800 degrees Celsius in presence of a limited amount of oxygen.

[0096] In some embodiments, the short path cracker is configured for performing flash pyrolysis of the feed material, on the surface of the reaction’s support heated to 400-600 degrees Celsius in presence of a limited amount of oxygen.

[0097] In some embodiments, the short path cracker is configured for performing flash pyrolysis of the feed material, on the surface of the reaction’s support heated to 500 to 550 degrees Celsius in presence of a limited amount of oxygen.

[0098] In some embodiments, the short path cracker is configured for performing flash pyrolysis of the feed material in the presence of an inert gas that is preferably steam and/or azote.

[0099] In some embodiments, the short path cracker is configured for performing flash pyrolysis wherein contact time between feed material and heated reaction’s support is less than 3 seconds, preferably less than 2 seconds and more preferably less than 1 second.

[0100] In some embodiments, the short path cracker is configured for performing pyrolysis, wherein the surface(s) of reaction’s support(s), wherein pyrolysis take place, are heated by several heating means that are preferably induction means, infra-red and hot gases.

[0101] In some embodiments, said heating means being positioned inside the enclosure. In some embodiments, said heating means being positioned inside the enclosure and/or in a zone of the enclosure having a reduced oxygen content that is preferably less than 1 % oxygen and/or in a zone of the enclosure being traversed by an inert gas.

[0102] In some embodiments, the surface of a reaction supports is heated by heating means that are induction and infrared means. [0103] In some embodiments, the surface of the reaction support, wherein cleaning means are positioned at least temporally in contact with the superior surface of the reactions supports.

[0104] In some embodiments, the short path cracker has cleaning means configured to clean at least part of the surface of the moving or rotating reaction’s supports wherein pyrolysis reaction take place, said cleaning means preferably comprising:

- at least one rake in permanent or temporally in contact with at least part of the surface of a reaction’s supports wherein pyrolysis takes place; and/or

- at least one rotating flail and/or brush in permanent or temporally contact with at least part of the surface of the reaction’s support means wherein pyrolysis takes place; and/or

- at least one ultrasonic means in permanent or temporally contact with at least part of the surface of the reaction’s support means in contact with part of the surface of a reaction’s supports wherein pyrolysis takes place; and/or

- at least one directed blow means blowing air, with low content in oxygen, or an inert gas in permanent or temporary contact with at least part of the surface of a reaction’s support wherein pyrolysis takes place.

[0105] In some embodiments, the feeding means is a feeding line mounted with spray nozzle’s.

[0106] In some embodiments, the feeding means is a feeding line mounted with spray nozzles: of the liquid feed type; and/or of the solid feed in form of small particulates type; and/or of the feeding stream liquid but containing solid particulates type.

[0107] A short path cracker, as defined in claim 38, for performing pyrolysis, wherein said spray nozzle being configured to spray, on the surface of the reaction’s support, drops of the liquid feeding oily stream having an average drop’s size of less than 10 mm, preferably of less than 5 mm, and more advantageously lower than 2 mm.

[0108] In some embodiments, said spray nozzle being configured to spray, on the surface of the reaction’s support, particulates having an average size less than 3 mm, preferably less than 2 mm, more advantageously the average size ranging from 0.5 to 1.5 mm.

[0109] In some embodiments, said spray nozzle being configured to spray, on the surface of the reaction’s support, a mixture of liquid and particulates with a ratio parliculates/liquid being in weight percent ranging from 5 to 100 %, preferably from 15 to 75 %. [0110] In some embodiments, the feeding means is a feeding line mounted with spray nozzle’s, spray nozzles being positioned to spray feeding oily feed material on the surface of a reaction’s support.

[0111] In some embodiments, the feeding means is a feeding line mounted with spray nozzle’s, spray nozzles being configured for spraying, on demand, a specific amount of feeding material, in order substantially or in order no liquid film would be able to form from the individual drops reaching the surface of the reaction’s supports.

[0112] In some embodiments, particulates and/or drops of the feeding material are sprayed to the reaction’s surface at a controlled pressure.

[0113] In some embodiments, the heating device is configured to heat the surface of the reaction’s support at a temperature ranging:

- in the case of particulates from 350 to 750 degrees Celsius, preferably from 450 to 600 degrees Celsius, more advantageously about 500 degrees Celsius; and

- in the case of a liquid feed advantageously from 300 to 650, preferably ranging from 450 to 550, and more advantageously at a temperature about 520 degrees Celsius.

[0114] In some embodiments, the heating device is configured to heat the surface of the reaction’s support at a temperature superior to the cracking temperature of the feeding material, said reaction’s support temperature being superior for preferably at least from about 5 to about 20 %, but more preferably between 5 to 10 %, to the cracking temperature of the feed material.

[0115] In some embodiments, the reaction support ends in a tube acting as a central rotating axle and wherein preferably higher end of the conical shape is supported on a bracket attached to the inner wall of the central body.

[0116] In some embodiments, the means used for bringing the solids outside the reactor is (are) entrainment with the gravity and/or, screw conveyors and/or, scoops and/or entrained with the vapors wherein preferably the means for bringing the solid outside the said reactor is by gravity by the exit tube.

[0117] In some embodiments, said reactor has two opposite exits: one for the solids at the bottom and one for the gas/vapors.

[0118] Also included is a process for producing liquid fuels and products from a starting material, that is preferably selected in the group constituted by oily feeds and/or by hydrocarbon feeds and/or by organic material in the form of agglomerates, in the form of agglomerated, said starting material, preferably having a reduced content in water, metal, glass and/or rocks, being thermally liquefied and further dewatered and the thereby obtained liquid fraction being thereafter submitted to a pyrolysis (preferably to a flash pyrolysis) treatment, performed in a short path cracker of the present application, and resulting in a gas fraction exiting the compact equipment, said gas fraction allowing, after a controlled liquid separation treatment, the recovering of liquid fuels.

[0119] In some embodiments, the agglomerates have, after drying and filtering, at least one of the following features:

- a humidity content lower than 75%;

- a content in metal and stones/glass representing both together representing less than 25 % weight percent of the total amount of agglomerates; and

- a total carbon content comprised between 30 % and 75 %.

[0120] In some embodiments, the feed can be in a form of pellets, granules and/or powder. In some embodiments, the agglomerates are in the form of pellets with an average weight ranging from 1 to 500 grams, when sprayed, less than 3 grams, preferably less than 1 gram, more preferably about 0.5 grams. In some embodiments, the agglomerates are in the form of pellets with a humidity content less than 60 %, preferably ranging from 5 to 65%.

[0121] In some embodiments, the recovered liquid fuels have a low sulphur content that ranges, according to ASTM D7544 - 12, from 0 a 5 %, preferably 0.03 % weight percent, preferably the sulphur content is lower than 0.05 %, more preferably lower than 0.03 %, and advantageously lower than 0.01%.

[0122] The present application also includes a process for producing liquid fuels from a starting material, that are waste hydrocarbons and/or organics material or a mixture of the two, said process includes: a) an optional preliminary dewatering step wherein water content of the starting material is reduced preferably to a value lower than 55 % and/or wherein particulate size of the starting material has been reduced to a size ranging from 3 mm to 0.1mm; b) a thermal step wherein at least partial liquifying and at least partial dewatering of the starting material, eventually obtained in previous steps a) occurs, is performed and wherein starting material is heated under:

- a pressure that preferably ranges from 0.3 to 1 atmosphere and this pressure is more preferably about 0.5 atmospheres, and

- at a temperature that is preferably lower than 250 degrees Celsius; c) a recovering step of the liquid fraction, resulting from step b), that may contain solid matters in suspension; d) a pyrolysis step (preferably flash pyrolysis step) wherein: o liquid fraction obtained in step b) and/or c), is treated in the short path cracker equipment, preferably under positive pressure and/or preferably in the presence of a sweep gas, that is advantageously an inert gas, and o reaction and straight-run products are recovered from the short path cracker equipment of the application, as vapors and as a gas mixture; and e) preferably the solids are taken out in the bottom of the short path cracker when there are chances of solids being entrained by the vapors an optional cyclone is included in the enclosure and optional infrared heater is put in the reactor, thus the vapors and gas exiting by the vapor exit are substantially clean of solids; and f) optionally, a condensation and/or fractionation step to obtain liquid fuel and gas, and wherein at least part of the liquid fraction recovered from step c), is added to the feeding stream preferably in order to adjust solid liquid ratio in the liquid feed stream entering the short path cracker.

[0123] The present application also includes a process for producing liquid fuels from starting material, that are waste hydrocarbons and/or organics material or a mixture of the two, said process includes: a) an optional preliminary dewatering step wherein water content of the starting material is reduced preferably to a value lower than 55 % and/or wherein stone and/or metallic content is reduced; b) a thermal step wherein at least partial liquifying and at least partial dewatering of the starting material eventually obtained in previous steps a), occurs and wherein starting material is heated under:

- a pressure that is preferably ranging from 0,1 to 10 atmosphere and more preferably this pressure is about 1 atmospheres, and

- at a temperature that is preferably lower than 270 degrees Celsius; c) recovering of the liquid fraction resulting from step b); d) recovering unliquified solid fraction from step b) and submitting said solid fraction to grinding in order to obtained particle with an average size preferably lower or equal to 4 mm, preferably ranging from 0.1 to 3 mm; e) mixing the fluid fraction obtained in step b) and the solid fraction resulting from grinding in a proportion that does not substantially affect the thermodynamic properties of the liquid fraction, the mixing results in a liquid containing solids in suspension; f) a pyrolysis (preferably a flash pyrolysis step) step wherein: o liquid obtained in step c) or e), is treated in a short path cracker, according to the application, preferably under positive pressure and/or preferably in the presence of a sweep gas, that is advantageously an inert gas, and o reaction and straight run products are recovered from the short path cracker as clean vapor-gas mixture; and g) preferably the solids are taken out in the bottom of the short path cracker when there are chances of solids being entrained by the vapors an optional cyclone is included in the enclosure and optional infrared heater is put in the reactor, thus the vapors and gas exiting by the vapor exit are substantially clean of solids; and h) a condensation and/or fractionation step to obtain liquid fuel and gas and products from the vapor-gas exiting the above part of the enclosure, and

- wherein, in the case wherein liquefaction in step c) is incomplete, the remaining unliquified solid fraction is incorporated in the liquid obtained in step c) preferably before entering the compact equipment and at concentration and/or particle size that does not affect significantly the physico-dynamic properties of the liquid entering the compact equipment; and

- wherein heavy hydrocarbon and/or heavy bio-oil fraction (antecedent) recovered from pyrolysis step is incorporated in liquid fraction resulting from step c), preferably in order to adjust the solid-liquid ratio in the liquid feed stream entering the preferably the solids are taken out in the bottom of the short path cracker when there are chances of solids being entrained by the vapors an optional cyclone is included in the enclosure and optional infrared heater is put in the reactor, thus the vapors and gas exiting by the vapor exit are substantially clean of solids; equipment.

[0124] A Process for producing liquid fuels from starting material, that are waste hydrocarbons and/or organics material or a mixture of the two, in a form of agglomerates, said process includes: a) a pre-treatment step wherein agglomerates, such as pellets and/or powder, are made from the starting material; b) an optional drying step, wherein agglomerates, obtained in the pre-treatment step a) or coming from the market and/or from waste collection, are dried to a water content lower than 55% weight percent; c) a thermal step wherein at least partial liquefying and at least partial dewatering of the agglomerates, obtained in previous steps a) and/or b), is performed, d) a pyrolysis step wherein: o liquid obtained in step c), is treated in a short path cracker of the application, preferably under positive pressure and/or preferably in the presence of a sweep gas, that is preferably an inert gas, and o reaction and straight run products are recovered from the short path cracker as solids and as a clean vapor-gas mixture;and e) a condensation and/or fractionation step to obtain liquid fuel and gas from the substantially clean vapor obtained in step d), and wherein, in the case wherein liquefaction in step c) is incomplete, the remaining unliquified solid fraction is incorporated in the liquid obtained in step c), preferably before entering the short path cracker at concentration and/or particle size that does not affect significantly the flow of the complex feed so it physico-dynamic properties to a fluid of the liquid entering the compact equipment.

[0125] Process, according to any one of claims 40 to 48, for producing liquid fuels from starting materials that are waste hydrocarbons and/or organics material or a mixture of the two, wherein at least one of the following pre-treatments is performed before feed material enters the compact equipment:

- solids present in starting material are broken into small pieces below 20 mm; and/or

- agglomerates are made of at least 75% by weight of organics or hydrocarbons mixed with water; and/or

- metals and rocks have been sorted out from the agglomerate, preferably by gravity and/or by magnetic separation; and/or

-the water content in the starting material is in weight less than 87% as during the (agglomeration) pelletizing part the water was taken out; and/or

- the solid content of the agglomerates (preferably pellets) has been, preferably before entering the second stage of the drying/liquefying step (step b), been increased to 15 to 30%, preferably by using a dry “Hammermill” that is for example of the Wackerbauer type); and/or

- the solid content is further increased, in a screw press, up to 50 to 60 % and eventually, with special system, such as separation mill, turbo dryer, high efficiency dryer, press, raised up to 85%; and/or

- dewatering is done with drum dryers or belt dryers to get to a lower water content. [0126] In some embodiments, in step c) of said process the partially dewatered and pre-treated feedstock is heated, preferably in a vessel, (at conditions of temperature and pressure allowing to: evaporate part of the water still present; and liquefy more than 50 % of the heavier hydrocarbons and/or organics present in the starting material, while managing control cracking of the feedstock under treatment.

[0127] In some embodiments, in step c): the water and lighter materials includes cracked material, such as proteins, fats and/or plastics, that are separated from the heavier portion that is at a liquid stage at operating temperature, allowing to eliminate water and to recover lighter material which can be further separated into gas and liquid with low solid content and used in a previous or, in a subsequent step(s), to further dry and or crack the feed stock and/or as fuel of any heating system and/or to be sold in a liquid form as a liquid fuel.

[0128] In some embodiments, in step c), the thermal separation treatment is performed in a vessel, at temperature to liquefy the most (this mean more than 70 %) of the hydrocarbons and/or organics and at a pressure that is preferably below the atmospheric pressure.

[0129] In some embodiments, in step c, the recovered lighter material is separated in two fractions:

- the first fraction that is a heavy diesel or bio diesel or fraction that falls back in the vessel; and

- the remaining fraction that is the light fraction of the lighter material is also separated into a liquid and gaseous or in at least 3 sub fractions: respectively in a liquid, solid, gaseous fractions.

[0130] In some embodiments, in step c): the water and lighter materials are separated from the heavier portion allowing to eliminate water and to recover lighter products which can be further separated and used as fuel.

[0131] In some embodiments, the transformation condition in the compact equipment are at least one of the followings:

- temperature ranges from 300 to 750 degrees Celsius;

- pressure lower the 2 atmospheres, preferably about 1.5 atmospheres;

- residence times range from 2 seconds to 2 hours, preferably from 5 seconds to 10 minutes, preferably about 3 minutes;

- the relative speed rotation of the reaction support and of the cleaning device ranges ranging from 0.1 to 200 t/minutes; and - spraying conditions being drop size ranging from 0,1 to 4 mm, preferably about 2 mm, more preferably about 1 mm, pression, the amount of feeding material being sprayed being preferably of about 250 kg per square meter and per hour,

- heating capacity being comprised between 50 et 600, 1(M) a 3(MX), preferably being about 200 KW per square meter and more preferably being about 100 KW in the case of cellulose and/or heavy oil;

- cooler or condensing surfaces condense products with higher boiling or sublimation boiling points

- the temperature of a drop is before being sprayed on the reacting surface lower than is cracking temperature but is higher than 110 degrees.

[0132] In some embodiments, in step e), the post treatment module is configured to perform the solid-gas separation, substantially without any condensation of the gas present in the solid gasmixture exiting the central module; and/or the post treatment module has preferably at least one cyclone and preferably two cyclones solids are further separated in a self-refluxing condenser; and/or finally, the vapours are condensed and separated either in a distillation column and/or in multiple condensers.

Claims

WHAT IS CLAIMED IS:

1. A process utilizing a short path cracker for pyrolyzing a feed material, wherein the feed material is selected from the group consisting of oily feeds, plastics, hydrocarbon feeds, and organic materials, and for recovering specialty products, feedstocks for plastics, and/or fuels, comprising:

• an enclosure having a substantially vertical lateral section, a bottom section, and a top section;

• feeding means comprising at least one spray nozzle configured to distribute the feed material as droplets or particles onto a reaction surface;

• a vapor exit preferably positioned at the top section of the enclosure to evacuate vapors generated during pyrolysis and/or optionally introduced inert gas;

• a solids exit positioned at the bottom section of the enclosure to remove solid residues;

• at least one reaction surface support within the enclosure, configured to conduct pyrolysis on at least part of its surface, said surface being conical and/or cylindrical;

• one or more surface cleaning mechanisms in contact with at least part of the reaction surface, wherein feed material is sprayed and pyrolysis occurs, for continuous cleaning of the reaction surface;

• internal and/or external heating means configured to heat at least part of the reaction surface;

• a vapor-solid separation device positioned between the reaction surface and the vapor exit;

• wherein a relative motion is induced between the cleaning mechanism and the reaction surface, such that: o the reaction surface support remains stationary while the cleaning mechanism moves, and/or o the reaction surface support moves while the cleaning mechanism remains stationary, and/or o both the reaction surface support and the cleaning mechanism move at identical or different speeds and/or in identical or different rotational directions;

• wherein pyrolysis occurs within the enclosure in an oxygen-depleted and/or inert gas environment.

2. The process of claim 1, wherein a reflux condenser is positioned inside the reactor enclosure between the reaction surface and the vapor-solid separation device.

3. The process of claim 1, wherein the majority of the feed material is pressurized and/or heated above its melting temperature or when many fine particulates are involved heated below their cracking temperature but below its cracking temperature prior to introduction.

4. The process of any one of claims 1 to 3, optionally incorporating self-cleaning condensing equipment.

5. The process of claim 4, wherein the self-cleaning condensing equipment consists of plate condensers mechanically cleaned using cleaning equipment such as brushes, scrapers, chains, and/or gas.

6. The process of claim 1, wherein optionally a reflux condenser is positioned inside the reactor enclosure between the reaction surface and the vapor-solid separation device.

7. The process of any one of claims 1 to 6, wherein the feed material is heated and/or pressurized using a screw conveyor, extruder, and/or pump prior to introduction into the reactor.

8. The process of any one of claims 1 to 7, wherein the feed material is sprayed at a temperature between 230°C and 470°C.

9. A short path cracker, as defined in any one of claims 1-8, wherein the reaction surface temperature is between 300°C and 800°C, preferably between 400°C and 600°C, and in an atmosphere essentially devoid of oxygen.

10. The short path cracker of claim 9, wherein for oily and plastic feed materials, the reaction surface temperature is between 300°C and 575°C.

11. The short path cracker of claim 9 or 10, wherein the enclosure has a cylindrical, quadratic, or triangular body, with a top section having a cylindrical or pyramidal form, and a bottom section having a conical or pyramidal form.

12. The short path cracker of any one of claims 9 to 11 , wherein the contact time between the feed material and the heated reaction surface is less than 2 minutes, preferably less than 1 minute, more preferably less than 3 seconds, and most preferably less than 1 second.

13. The short path cracker of any one of claims 9 to 12, wherein the reaction surface is heated by one of different heating sources, preferably induction, infrared, burners and/or hot gases.

14. The short path cracker of any one of claims 9 to 13, wherein the feeding means consists of one or more feeding lines equipped with one or more spray nozzles.

15. The short path cracker of any one of claims 9 to 14, wherein the cleaning mechanism consists of multiple brushes and/or blades for continuous cleaning of the reaction surface.

16. The short path cracker of any one of claims 9 to 15, wherein the feeding means consists of a feeding line with spray nozzles, configured to spray predominantly liquid or oily feed material onto the reaction surface.

17. The short path cracker of any one of claims 9 to 16, wherein the reaction support terminates in a central rotating tube, with the higher end of the conical reaction surface supported by a bracket attached to the inner wall of the enclosure.

18. The short path cracker of any one of claims 9 to 17, wherein solid removal is achieved by gravity, screw conveyors, scoops, and/or vapor entrainment, preferably by gravity through an exit tube.

19. A process including a short path cracker, for performing pyrolysis on a feed material, preferably selected in the group constituted by oily feeds, plastics and/or by hydrocarbon feeds and/or an organic material, and for recovering specialty products, feedstock to make plastics and/or fuels, said equipment comprising: an enclosure having a lateral part substantially vertical, a bottom part and a superior part, said enclosure comprising at least; feeding means, lines spray nozzles, positioned to distribute the feed material in droplets particles on the reaction surface; a vapor exit positioned preferably in the superior part of the enclosure and for evacuating vapors generated during the pyrolysis and/or added inert gas; a solids exit positioned preferably in the bottom part of the enclosure and for evacuating solids, at least one reaction’s support preferably positioned inside the enclosure, for performing pyrolysis on at least part of the surface of the reaction’s support, said reaction surface having at least partially a conic and/or cylindrical shape, one or several surface cleaning devices positioned inside the enclosure and configured to be in contact with at least part of the reaction surface wherein feed material is sprayed and wherein the pyrolysis reactions take place, for cleaning at least part of the surface and internal and/or external heating means configured for heating at least part of the reaction surface: a vapor/solid separation device situated in the enclosure between the reaction surface and vapor exit wherein the reaction’s surface support and the heating means are preferably closely positioned;

- wherein a relative movement is initiated between cleaning means and the reaction’s support: and

- wherein the reaction’s support is stationary and the cleaning means are moving relatively; and/or

- wherein the reaction’s support is moving and the scraping device is stationary; or

- wherein the reaction support and the cleaning means are moving according to identical or different speeds and/or according to identical or different rotation directions and/or according to different;

-wherein said equipment is optionally configured for the pyrolysis to be performed in the enclosure preferably containing one or more inert gas and/or oxygen poor atmosphere.