Pyrolysis of organic waste - Equipment for thermocatalytic decomposition

Abstract

Apparatus for thermal catalytic decomposition - pyrolysis of organic waste. The present specification provides an apparatus for thermal catalytic decomposition - pyrolysis of organic waste, comprising a reservoir connected to a reactor by a supply line, a valve disposed in the line, the reactor containing a heating element and / or a radiation source located up to a maximum level corresponding to approximately 1 / 3 of the height from the bottom of the reactor, and a temperature sensor located up to a maximum level corresponding to 1 / 3 of the height from the bottom of the reactor, an output line protruding from the reactor lid to which a cooler is connected, the end of the output line being connected to an orifice of a receiver for containing liquefied product via a branch for discharging product gas.

Description

[Technical field]

[0001] The present invention relates to an apparatus for pyrolytic (thermally) decomposing organic matter, and to the pyrolysis oil produced by this process. The present invention combines two scientific disciplines: physics and chemistry. [Background technology]

[0002] Manufacturers of non-renewable resources are currently facing strong pressures to restrict the use of non-renewable resources such as oils and other fossil carbon sources involved in the production of liquid fuels, mainly for ground transport purposes. Fuels for spark-ignition engines in automobiles mainly include bioethanol, produced by fermenting agricultural crops with a high carbohydrate content, and fatty acid methyl esters, produced by re-esterification of vegetable oils or optionally animal fats. The production of fuels using renewable resources formed by hydrocarbons obtained by hydrogenation of vegetable oils (HVO) is small. The usable properties of bioethanol and fatty acid methyl esters are worse in certain respects compared to the properties of classical fossil fuels: bioethanol is mainly characterized by its miscibility with water and the resulting fuel quality deterioration over long storage periods, together with the ingress of air humidity, which deteriorates the fuel quality during long storage periods. Methyl esters suffer from poor storage stability and thermo-oxidative stability. These usable properties during the production of hydrogenated vegetable oils and their use in compression ignition engines are quite good, leading to high hydrogen consumption and short service life of the hydrogenation catalysts essential in the production process.

[0003] At present there are no further options for producing liquid fuels from common renewable resources. The production of liquid fuels is expected to utilize various types of biomass. This mainly deals with pyrolysis or thermo-catalytic decomposition, a process that forms substances with lower boiling points corresponding to the boiling range related to the usual liquid fuels. The products obtained by such decomposition must be further processed to ensure that the resulting properties meet the requirements for the quality of the final product distributed among consumers. Another procedure to those mentioned above is pyrolysis, which produces synthesis gas and subsequently synthesizes hydrocarbons suitable for producing liquid fuels.

[0004] US Patent No. 5,993, 167 describes the pyrolysis of vegetable oils and animal fats in an apparatus featuring a skim-absorbent film on the heated interior surface of a pyrolysis reactor. US Patent No. 5,993, 171 describes the utilization of a deoxidizing agent mixed with various vegetable oils and other biological feedstocks in a reactor that is subject to the effects produced by an electromagnetic field while equipped with a radiation source that transmits a predetermined amount of energy in the infrared spectrum. Other patented procedures include catalysis during the decomposition of the feedstock.

[0005] For example, US Patent No. 3,999,666 describes a method for pyrolysis of organic oil-based feedstocks in contact with calcined dolomite used as a catalytic agent. US Patent No. 4,243,823 describes the production of pyrolysis oil by two-stage thermocatalytic decomposition of waste in an apparatus including a pretreatment zone and a pyrolysis zone of the treated material. US Patent Application Publication No. 20190144758 describes the pyrolysis of vegetable oil and other liquid feedstocks inside a tube furnace by injecting the feedstock through a nozzle for ultrasonic atomization of the injected material. The injection of the feedstock into the reactor is performed in parallel with the introduction of ammonia, methanol, or hydrogen. Part of the reactor also contains a catalyst bed filled with materials based on zeolites, metal oxides, solid acids, and alkaline catalysts. Apart from the specific configurations of various reactors for the pyrolysis of vegetable oils and other materials, traditional refining techniques are also detailed, as disclosed in US Patent No. 5,243,823. In said specification, the feedstock cracking is carried out in a fluid catalytic cracking (FCC) unit featuring a classical cracking catalyst, the pyrolysis stage is followed by its cyclic regeneration process.

[0006] When pyrolysis is carried out to produce a liquid fraction to be utilized in further processing with the goal of producing high quality engine fuel, for example, the desired result is to maximize the yield from the liquid phase at the expense of gas, coke, or possible unreacted feedstock. Cracking conditions (high temperature, coproduction of pyrolysis gases) are usually accompanied by the ingress of any undecomposed particles of feedstock into the product, which therefore needs to be returned to the pyrolysis process. [Prior art documents] [Patent documents]

[0007] [Patent Document 1] Czech Specification No. 306462 [Patent Document 2] European Patent No. 2129746 [Patent Document 3] US Patent Publication No. 20110289826 [Patent Document 4] European Patent No. 3132004 [Patent Document 5] US Patent Publication No. 20070007176 Summary of the Invention [Problem to be solved by the invention]

[0008] Subject of the Invention The solution presented here is applied according to the invention to a device for carrying out a change in the chemical structure within the cells of an original organic material, advantageously in liquid state, forming a different cellular structure if necessary, and establishing entirely new cells of the organic material. This change can affect not only the original structure, but also the original state of the material. The cells referred to in this case contain, in the simplest case, chemically determined particles of organic material.

[0009] For the purposes of this description, physicochemical thermocatalytic process (decomposition) refers to the breakdown of the cellular structure of the original material when subjected to the effects of temperature and radiation, simultaneously utilizing a temperature gradient.

[0010] The object of the present invention is to process the original feedstock by utilizing specific equipment and undemanding technological conditions (carried out at atmospheric pressure and without the presence of hydrogen), with or without a deoxidizer, or optionally using a catalyst, to obtain products with lower molecular weight and higher hydrocarbon content, or low residual oxygen content, suitable for subsequent refining to produce the respective engine fuel components.

[0011] The oxygen contained in the ester groups of the triglycerides of fatty acids is released in the form of carbon monoxide and carbon dioxide during the deoxidation-oxidation reaction. The extent of deoxidation is assisted by added residual petroleum fractions, and a significant reduction in the oxygen group content has been achieved by catalyst supplementation in the reaction mixture. [Means for solving the problem]

[0012] The subject of the present invention is an apparatus for the thermal catalytic decomposition-pyrolysis of organic waste, comprising: The device comprises: Supply Line 2 By reactor 4 A waste reservoir connected to 1 And the line 2 Valves to ensure control of waste volume 3 are placed, Reactor 4 The reactor 4 Waste located outside or inside the reactor 4 Bottom 7 Heating element for heating to a maximum level equivalent to approximately 1 / 3 of the height from the 5 and / or radiation source 5a Including, Reservoir 1 and, a temperature sensor (6) located near the heating element and / or radiation source for controlling the amount of power supply, the temperature sensor (6) being located up to a maximum level corresponding to 1 / 3 of the height from the bottom (7) of the reactor (4), an output line (10) protruding from the lid (9) of the reactor (4) for conveying the gaseous components of the product obtained, and connected to a condenser (16) for liquefying the gaseous components of the product obtained; Output Line 10 The end of the gas turbine is connected to a branch for discharging product gas. 21 a receiver for containing the liquefied product via 17 connected to the orifice of Includes the device.

[0013] Output Line 10 Sensor on top 11 and cooler 16 A preferred configuration includes a reactor 4 US20100233633A1 - Control sensor for controlling the chemical composition of gas leaving the - Google Patents 12 and the sensor 11 and the cooler 16 A throttle flap valve for controlling the gas flow rate located between13 and said output line 10 There is also a follow-up cooler inside 16 and reflux section 15 Intercooler connected to both 14 is further arranged, and the reflux section 15 Heating element 5 Outside the reactor 4 is connected into the orifice of the

[0014] Furthermore, in an advantageous embodiment, a temperature sensor is provided for establishing the temperature of the gaseous components obtained from the waste. 8 A reactor comprising: 4 The upper half of the device is characterized by:

[0015] For the purposes of this invention, waste is not a specific waste per se but includes organic materials for non-food uses.

[0016] One embodiment of the invention is a sensor for the temperature and flow of a gaseous product component. 11 Output line with convenient form 10 Includes.

[0017] The number and location of sensors in an apparatus according to the invention is preferably determined by the conditions for carrying out the method, the type of apparatus and the specific type of raw material or mixture of raw materials, including any possible additives, to be processed in the particular apparatus.

[0018] radiation source 5a is located inside the reactor, preferably just below the waste level, while the reactor 4 The highest point of the level within the reflux area 15 reaches just below.

[0019] The form and shape of the radiation source must provide an optimum reaction surface depending on the size and shape of the reactor and the desired decomposition rate. Advantageous components include internal reactor surfaces that are helical, double or multiple twisted helical, helical, or tapered, or any combination of these within the reactor.

[0020] Another advantageous embodiment is a heating element further comprising an induction element or a gas burner. 5 This includes devices having the following:

[0021] In another advantageous embodiment according to the invention, the reactor 4 is Supply Line 2 It is preceded by a supply line 2 But the waste reactor 4 A preheater to ensure that the waste is preheated before entering the 18 It is equipped with:

[0022] The line before the reactor is preferably equipped with a level gauge. 20 T-joint for providing 19 A level gauge 20, preferably made of glass, is fitted within an orifice in the reactor lid as an indicator of the content level inside the reactor.

[0023] Yet another embodiment of the present invention is the reactor 4 In the vicinity of the radiation source 5a inside the reactor, a closing grid is provided to ensure an airtight sealing of the reactor and prevent any oxygen from passing through. 22 The present invention is characterized in that it is configured using the following:

[0024] An advantageous embodiment of the present invention also provides a feedstock reservoir 1 but containing wastes enriched by up to 20 weight percent with predominant amounts of high boiling point hydrocarbons and other organic substances, such as distillation residues and vacuum distillates of oil origin, and more preferably provided with a catalyst based on an alkali metal hydroxide, most preferably a mixture of KOH and NaOH.

[0025] The entire apparatus is constructed from stainless, heat and chemical resistant steel with fiberglass insulation. The electrical feeds provided for the heating elements inside the reactor are fitted with ceramic grommets.

[0026] Convenient reactors for the pyrolysis are especially pot or tubular reactors.

[0027] The feed level inside the reactor was appropriately checked using a glass level gauge attached by a suitable metal capillary forming impulse piping between the top of the reactor and the flat bottom of the reactor vessel which was connected to a reservoir holding fresh feed.

[0028] A thermometer well, preferably equipped with a thermoelectric subsection, was provided in the apparatus to ensure measurement of the temperature below the feed level, the temperature of the steam above said level, and the temperature of the steam exiting the reaction piping before entering the water cooler.

[0029] Actual reaction progress Phase 1: Launch This step involves providing the material to be transformed together with other materials specifically required for this transformation, either forming a homogeneous or heterogeneous mixture or added on an individual and stepwise basis.

[0030] The initial energy required for initiating the decomposition and further transformation of the raw materials is supplied to the reactor either via an internally provided radiation source, i.e., a radiation source located within the space for the best and fastest development of such initiation conditions, or by delivering energy into the reaction space by inductive heating from the outside, with the energy being directed to the inner shell of the reactor or to a radiation source 5a located inside the reactor, or by a combination of these heating options, a gas-powered heat supply, or another available heat supply.

[0031] The initiation impulse is defined by utilizing the temperature difference or by supplying energy to such an extent that it allows the pyrolysis of the individual substances. Once a certain temperature is reached, the substances are subjected to pyrolysis, followed by the pyrolysis of other substances present inside the reactor. At this stage, all the substances are transformed into a gaseous state, reaching a temperature of 60 to 600 °C.

[0032] Second stage: Propagation a) Reaction pathways and their partial control inside the reactor As the radical reactions proceed, there are complex mechanisms at work to carry out the coalescence and decomposition process, but various intermediates or products are formed and subsequently decomposed until the final reaction stage, i.e., completion, occurs when the final residues of gaseous radicals are cooled to a temperature level where they stop further decomposition and begin to interact.

[0033] This section of the reactor utilizes feedback impulses to control other technology segments by having sensing elements (measurement sensors) to monitor time, pressure, temperature, volume, flow rate, and feedback from the individual components for this technology, thus maintaining the set conditions for the reaction.

[0034] Thus, the reaction is not directly controlled using calculated chemistry, but rather indirectly controlled through optimal conditions established for the particular reaction within tolerance levels that have little effect on the course of the reaction.

[0035] Data received from the individual sensors during the course of the reaction is monitored and compared to verify process compliance, along with possible deviation ranges and their possible impact on the quality of the final product.

[0036] b) The course of the reaction and its evaluation by possible measurements outside the reactor When the still interacting individual radicals leave the reactor in the form of hot gases, still using the evaluation of the data from the individual measurement sensors, the compounds which are the object of production, as well as compounds which are not currently desired in the final product, are captured by partially selecting them and returned to the reaction space, where they are subsequently chemically reacted to produce the compound desired at that particular time.

[0037] Part III: End The next termination stage of the chemical transformation is the rapid cooling of the hot gases, which stops the radical reactions, providing that the existing products no longer change and that their composition remains constant and extremely stable, whilst being suited to the compounds to be produced.

[0038] Further processing of the compounds produced then involves treating or upgrading them as required in liquid, gaseous or solid state, as applicable.

[0039] As preferably used to produce fuels and lubricants from renewable resources, particularly feedstocks of plant origin, the process can produce extremely pure hydrocarbons with carbon chains of the same or optionally different lengths as the original feedstock, as well as compounds that contain various combinations of the elements present in the original material, such as FFAs (free fatty acids), alcohols, phenols, ketones, glycerin, esters, and other materials that contain primarily carbon (C), hydrogen (FI), oxygen (O), nitrogen (N), phosphorus (P), calcium (Ca), or potassium (K).

[0040] The principle is based on partially controlling the course of radical reactions in a specific device, i.e., reactor, essentially taking advantage of the differences in ignition or thermal decomposition points of the individual substances entering the reaction, the homogeneity as well as the heterogeneity, or the aggressiveness of one of these substances so strong that it can disrupt the molecular cell structure in the other feedstock to initiate the radical reaction.

[0041] Based on creating specific time, temperature, pressure, and other conditions to facilitate the radical reaction in the reaction space and the subsequent cooling of the resulting gas at a specific time, the structure of the organic composition induced by said conditions is produced precisely as desired.

[0042] The chemical structure of the initial organic material is thus altered using a multifunctional device, i.e., a pyrolysis reactor, and the subsequent processing of the resulting chemicals involves several subsequent moieties to cause such alteration to occur gradually.

[0043] Pyrolysis at higher temperatures without oxygen flow converts the initial organic material containing carbon, hydrogen, or optionally oxygen and other elements into mainly liquid pyrolysis products (pyrolysis oil), pyrolyzed gases, or optionally solid carbon residue. The yield ratio of these products depends on the composition of the feedstock and the process conditions, especially the temperature and the reactor retention time. The average molecular weight of the compounds contained in the pyrolysis oil is low compared to the initial feedstock. Possible feedstocks include used cooking oils, animal fats and oils, and other liquid mixtures of organic origin, preferably alone or in mixtures of liquid substances.

[0044] The pyrolysis oil produced can preferably be used to produce liquid fuels.

[0045] One of the advantageous embodiments of the device for carrying out the pyrolysis (thermal decomposition of materials) of organic origin, in particular waste, comprises a specific part of a preheating device for the feedstock, a pyrolysis reactor, a partial condenser unit and a condenser for the pyrolysis oil. The preheating of the feedstock is carried out by an exchanger, where the feedstock is preheated at 200 ° C to 400 ° C. Following the preheat exchanger, the material enters the pyrolysis reactor, where further heat is provided to ensure the decomposition reaction at 250 ° C to 430 ° C. The products obtained by the decomposition are extracted in the vapor phase into a cooler, where partial condensation occurs, accompanied by the part with the highest boiling point. These parts are then remixed with the feedstock and enter the pyrolysis reactor. The amount of product that has not been condensed inside the cooler due to partial condensation is discharged into another cooler (heat exchanger), whereby it undergoes complete condensation, except for the pyrolysis gases. There is also a small amount of uncracked feedstock containing solid parts (coke) that are continuously extracted from the pyrolysis reactor.

[0046] Prior to entering the reactor, the feedstock is preferably mixed with most of the high boiling hydrocarbons and small amounts of material containing other organic materials, such as oil-derived distillation residues and vacuum distillates, soot, or charcoal.

[0047] The energy required to bring the feedstock to the cracking temperature level is supplied to the pyrolysis reactor either directly using a radiation source located inside the reactor or indirectly by an induction heating installation, in which the required energy is transferred onto a radiation source using a coil located outside the reactor space. This reactor heating method can be combined with a separate heating unit featuring a solid fuel burner. Such a burner can preferably use the gaseous portion of the product obtained by pyrolysis.

[0048] The unreacted feedstock portion containing insoluble material (coke) is extracted from the bottom of the pyrolysis reactor to ensure that insoluble material does not accumulate inside the reactor during continuous operation of the unit.

[0049] The pyrolysis using the procedure carried out in the apparatus described herein can be adapted by influencing the composition of the product obtained by pyrolysis, mainly in terms of the content of unsaturated hydrocarbons and oxygen species, by adjusting the process conditions, in particular the reaction temperature of the pyrolysis, the level height inside the pyrolysis reactor, the retention time, the temperature of the partial condensation cooler, and the amount of added material containing high-boiling hydrocarbons and other organic substances.

[0050] The composition of the pyrolysis product can also be influenced to reduce the content of oxygen species by adding catalysts to the pyrolysis reactor, as catalysts melts of hydroxides of alkali metals, mainly Na and K, have been used.

[0051] As far as the terms heterogeneous and homogeneous deacidification are concerned, homogeneous deacidification involves deacidification agents that are miscible with the liquid feedstock (petroleum distillation residues). Heterogeneous deacidification deals with immiscible ones (soot, coke with oil, or vice versa, straw, sawdust with asphalt).

[0052] For purposes of this invention, a deoxidizer is a raw material having a high excess carbon content, added in a predetermined ratio to the initial feedstock intended for deoxidation to affect the deoxidized final product.

[0053] For the purposes of the present invention, deoxidation is understood as a process that occurs in this device to heat the carbon contained in the deoxidizer to its ignition point, with the environment protected from oxygen circulation, and to hold the heated carbon in order to strip the initial feed of the oxygen necessary for its ignition, collapsing the cells of the initial feed and initiating radical reactions, as a result of which the initial feed is deoxidized, decreasing its content of oxygen compounds while increasing its content of pure hydrocarbons. [Brief description of the drawings]

[0054] [Figure 1] FIG. 1 shows a first embodiment of the apparatus defined in the present invention - an unconnected reflux pot reactor. [Diagram 2]FIG. 2 shows a diagram of a second embodiment of the apparatus defined in the present invention - a pot reflux reactor (homogeneous deoxidation). [Diagram 3] FIG. 3 shows a diagram of a third embodiment of the apparatus defined in the present invention - a pot reflux reactor (heterogeneous deoxidation). [Figure 4] FIG. 4 shows a fourth embodiment of the apparatus defined in the present invention - a tubular reflux reactor. [Figure 5A-5D] 5A, 5B, 5C, and 5D show the FTIR spectra of samples PL8, PL9, PL10, and PL11. [Fig. 5E-5G] 5E, 5F, and 5G show the FTIR spectra of samples PL12, PL13, and PL14. [Figure 6] FIG. 6 is a graph showing absorbance versus wave number for Samples 1 to 4. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0055] Working Example Input materials subjected to pyrolysis: Food quality oil: Rapeseed oil: Density at 15°C: 919.1 kg.m-3 Dynamic viscosity at 40℃: 39.8 mm2s-1 Ignition point: 235℃ Palmitic acid: 3.8% by weight Palmitic acid: 3.8% by weight Oleic acid: 61.8% by weight Linoleic acid: 32.3% by weight Sunflower oil: Density at 15°C: 919.1 kg.m-3 Dynamic viscosity at 40℃: 38.3 mm2s-l Ignition point:>250℃ Palmitic acid: 7.6% by weight Stearic acid: 4.9% by weight Oleic acid: 21.1% by weight Linoleic acid: 66.4% by weight Russian Export Mixture (VZ PSP, Litvinov refinery) petroleum vacuum residue (VR): Penetration: 213 pu Density: 1006.2 kg.m-3 Viscosity at 100°C: 1850 mPa.s Viscosity at 150°C: 156 mPa.s Asphaltene content: 5.8% by weight Sulfur content: 2.1% by weight Bottoms from a mixture of Azeri Light and CPC Petroleum (Kralupy n. Vlt. refinery): Density: 960.5 kg.m-3 Viscosity at 100°C: 180 mPa.s Sulfur content: 2.1% by weight

[0056] Specific embodiments of the device according to the invention Example 1: Unconnected Reflux Pot Reactor (see FIG. 1) Reservoir 1 is the supply line 2 This supply line is provided with a control valve 3 Through the pot reactor 4 The feed line delivers a liquid feedstock (vegetable oil - food quality) which is fed to a radiation source. 5a The pyrolysis is carried out in the temperature range of 380-430°C using a radiation source. The radiation source comprises a resistive wire just below the liquid level to be pyrolyzed, i.e. approximately 1 / 4 above the bottom of the reactor. Meanwhile, the pyrolysis temperature range is monitored by a sensor 6, which comprises a thermocouple in a thermowell, preferably made of glass, to indicate the content level inside the reactor, and which is bonded to the reactor lid.

[0057] The level of the raw material inside the reactor is preferably monitored using a level gauge 20. The level gauge is preferably made of glass and is4 Lid 9 The level gauge is connected to an orifice in 20 is preferably a T-joint located before the reactor 19 are joined by

[0058] The temperature of the generated pyrolysis gas is measured by the sensor. 8 Measured using the output line 10 The sensor 11 , and then directing such gas to a cooler. 16 The remaining gaseous portion of the hydrocarbons is cooled and liquefied inside the component. 21 through the liquid product receiver 17 is released from

[0059] Example 2: Pot Reflux Reactor (Homogeneous Deoxidation) (See FIG. 2) Deacidification agent - petroleum distillation residue and vegetable oil are used. Distillation residue is 4 The deoxidizers-petroleum distillation residue and vegetable oil are used so that they are charged into the reactor and preheated to a temperature close to their intensive cracking point (approximately 410°C). 4 The input line 2 before the preheater is preferably 18 It is equipped with:

[0060] A catalyst comprising a mixture of KOH and NaOH is preferably added. Once a temperature of 410°C is reached, the radiation source located just below the stillage level is powered on and a quantity of a mixture containing oil and 5% stillage or soot is introduced into the reactor.

[0061] The following three sensors are present in the space filled with distillation residue (soot). 1) Temperature sensor for monitoring still bottoms 6 , the feedback switches on possible cooling. 2) Temperature sensor for stillage level 6b, the feedback increases the supply of reaction mixture so as to maintain an efficient radiation source submerged nearly all the time. 3) Radiation source 5a Temperature Sensor for 6a , the feedback increases the power input of the radiation source if the temperature decreases. Sensors located inside the reactor: 4) A temperature sensor to monitor the product vapors generated inside the reactor. 8 , Sensors installed after the reactor: 5) A sensor after the reactor for monitoring the gas mixture and its compliance with the expected composition (target state) at the time of gas discharge into the cooler. 11a The feedback opens a flow path to a reflux device or directly into a condenser. The reflux device has an outlet for returning all the abovementioned boiling parts into the reaction space.

[0062] Sensors 11 and cooler 16 The output line between 10 is the reactor 4 and throttle flap valve 13 and a control sensor for controlling the chemical composition of the gas exiting the 12 This adjusts the flow rate of gases connected in parallel, while the output line 10 In addition, an intercooler 14 The intercooler is equipped with a 16 , as well as a heating element 5 Outside the reactor 4 1 and the reflux section 15 connected to the

[0063] Example 3: Pot reflux reactor (heterogeneous deoxidation) (see FIG. 3) The process used deoxidizers - stillage and vegetable oil. In this case coal (coke) is charged into the reactor and preheated to a temperature of approximately 700°C. A catalyst comprising a mixture of KOH and NaOH is preferably added. Once a temperature of 700°C is reached, a radiation source located just below the stillage level is used. 5a The power was turned on and a predetermined amount of a mixture containing oil and 5 wt. % distillation residue or soot was introduced into the reactor.

[0064] This differs from Example 2 in that the process involves heterogeneous deoxidation.

[0065] Pot Reactor 4 The heat supplied to the hopper 23 and shutoff valve 24 whereby coal or coke is fed into the device and subsequently preheated to a set temperature of 700°C.

[0066] Regarding the technology used, the device also 22 and the grid needs to be hermetically sealed from the surrounding environment.

[0067] The ash discharge below the reactor is performed by a flap valve. 25 This is ensured by

[0068] The following three sensors are present in the space filled with distillation residue (soot). 1) Temperature sensor for stillage 6 , the feedback switches on possible cooling. 2) Level sensor for raw material - coal (coke) 6b The feedback keeps the source submerged in the feedstock by aligning the feedstock. 3) Temperature sensor for radiation source 6a , the feedback increases or decreases the power input. Sensors located inside the reactor: 4) Temperature sensor for the temperature of the gas generated inside the reactor 8 , 5) Sensors for temperature and flow rate of the produced gas 11 ,Feedback for mixture dosing. Sensors installed after the reactor: 6) A sensor after the reactor at the gas discharge into the cooler to check the gas mixture conformity to the expected composition (target state) 11a The feedback opens the input into a reflux device or directly into a cooler. The reflux device has an outlet for returning all the abovementioned boiling parts into the reaction space.

[0069] Example 4: Tubular reflux reactor (see FIG. 4) A heating element including an induction element (optionally a solid fuel burner) 5 heated the entire surface of the tubular reactor and, when the entire surface had reached the reaction temperature, this surface was sprayed uniformly with a mixture consisting of oil and deoxidizer-distillation residue (or soot). The proportion of distillation residue in this case amounts to 5-70% by weight relative to the total mixture weight.

[0070] 1) Temperature sensor for the reaction surface 6a , providing feedback to increase or decrease the power input. 2) Gas temperature sensor 6 , providing feedback to increase or decrease the ingredient dosing rate. 3) Temperature sensor for the gas generated inside the reactor 8 , 4) Sensors for temperature and flow rate of the produced gas 11 , controlling the mixture dosage and providing feedback to increase or decrease the pressure inside the reactor (or optionally the reaction time inside the reactor). 5) A sensor after the reactor at the gas discharge into the cooler to check the gas mixture and its compliance with the expected composition (target state). 11a , the feedback opens the input into a reflux device or directly into a cooler. The reflux device has an outlet for returning all of the abovementioned high boiling fractions into the reaction space.

[0071] The resulting products were analyzed using FTIR spectroscopy (Fourier Transform Infrared Spectroscopy) shown in Figures 5A, 5B, 5C, 5D, 5E, 5F, and 5G. [Table 1]

[0072] In the FTIR spectra of the individual samples as shown in Figures 5A, 5B, 5C, 5D, 5E, 5F and 5G, the detailed table below mentions the area ratio of the bands in the FTIR spectra corresponding to carbonyl and carboxylic acid groups relative to the band regions corresponding to carbon framework groups of both single hydrocarbons as well as hydrocarbon strands of separate compounds, i.e., carboxylic acids, esters of carboxylic acids, etc. The use of catalyst in the feed significantly reduced the carbonyl and carboxylic acid groups in the final products (PL12-PL14). [Table 2]

[0073] The figure below shows examples of infrared spectra obtained by analyzing the products from the final test stage. The batches include samples 1 to 4. Samples 3 and 4 were obtained when sodium-based catalyst was added in the reaction mixture. Samples marked as samples 1 and 2 serve for reference. The presence of the additive had a positive effect that can be summarized as follows. The spectra can be interpreted by the spectral band ranges at 1700 and 2900 cm-1 to conclude the content of the compounds. The oxygen in these samples already reaches less than 10 percent. The samples mainly contain saturated hydrocarbon chains, indicated by the low band of C=CH vibrations at 3100 cm-1.

[0074] The product composition can be influenced by adjusting the reaction conditions, or optionally the feed composition, the addition of catalysts, or any other oxidizing, hydrogenating, or deoxidizing and dehydrogenating agents. [Industrial Applicability]

[0075] The present invention may be utilized in refineries, petrochemical, chemical, waste management and environmental protection industries, as well as specialty chemical plants. [Explanation of symbols]

[0076] 1 Reservoir 2 Supply Line 2a Supply Input Line 3 Valve 4. Reactor 5 Heating Elements 5a Radiation source 6 Temperature Sensor 6a Radiation source temperature sensor 6b Material level temperature sensor 6b Distillation residue monitoring level sensor 7. Bottom of reactor 8 Temperature sensor for the exhaust gas after the reactor 9 Reactor Lid 10 Output Line 11 Temperature and flow rate sensors 11a Gas mixture composition check sensor 12 Control Sensor 13 Throttle flap valve 14 Intercooler 15 Reflux section 16 Cooler 17 Receptor 18 Preheater 19 T-joint 20 Level Gauge 21 Branch for product gas discharge 22 Closed Lattice 23 Coal (coke) reservoir 24 Close flap valve 25 Ash discharge flap valve

Claims

1. An apparatus for the thermocatalytic decomposition-pyrolysis of liquid organic waste, comprising: The apparatus, a reservoir (1) for waste material connected to a reactor (4) by a supply line (2), in which a valve (3) for controlling the amount of said waste material is arranged, said reactor (4) comprising a heating element (5) for heating said waste material and a radiation source (5a), said heating element (5) being located outside said reactor (4) to a maximum level corresponding to about 1 / 3 of the height from the bottom (7) of said reactor (4), and said radiation source (5a) being located inside said reactor (4) and capable of being immersed in said waste material, which is liquid organic matter, said radiation source (5a) being a resistance wire in the form of a helical, double or multiple twisted helix; a temperature sensor (6) located near the heating element and / or the radiation source and located up to a maximum level corresponding to 1 / 3 of the height from the bottom (7) of the reactor (4), an output line (10) protruding from the lid (9) of the reactor (4) for conveying the gaseous components of the product obtained, to which is connected a condenser (16) for liquefying the gaseous components of the product obtained; 1. The apparatus according to claim 1 , wherein the end of the output line (10) is connected to an orifice of a receiver (17) for containing the liquefied product via a branch (21) for discharging the product gas, and the output line is equipped with a sensor (11) for monitoring the temperature and flow rate of the gaseous components of the product obtained, and the sensor (11) and the cooler (16) are configured to have the output line (10) including a sequential arrangement including a control sensor (12) for checking the chemical composition of the gas leaving the reactor (4) and a throttle flap valve (13) for controlling the gas flow rate located between the sensor (11) and the cooler (16), and further an intermediate cooler (14) is arranged in the output line (10) connected to both the cooler (16) and a reflux part (15), the reflux part being connected outside the heating element (5) into the orifice of the reactor (4).

2. The apparatus described in claim 1, characterized in that the upper half of the reactor (4) is provided with a temperature sensor (8) for determining the temperature of the gaseous components of the product obtained from the waste.

3. The device described in claim 1, characterized in that the heating element (5) is an induction element or a solid fuel burner.

4. An apparatus as described in any one of claims 1 to 3, characterized in that the supply line (2) is provided with a preheater (18) for ensuring that the waste is pre-heated before it enters the reactor (4).

5. An apparatus as described in any one of claims 1 to 4, characterized in that the supply line (2) is provided with a T-shaped fitting (19) for connecting a level gauge (20) indicating the level height of the waste inside the reactor (4), and an orifice for the level gauge in the lid (9) of the reactor (4).

6. 6. Apparatus according to any one of claims 1 to 5, characterized in that it comprises a closing grid (22) arranged inside the reactor (4), close to the heating element (5), to ensure hermetic sealing of the reactor (4) and the prevention of the ingress of oxygen.

Images