The object of the invention is a method of receiving, fractioning and condensing gas mixtures, particularly hydrocarbon formed during thermo-catalytic degradation of plastics (particularly polyolefin or with high content of this group of materials) and a set of devices for implementing the method.

A mixture of hydrocarbon vapours produced in the process of thermo-catalytic degradation of the dirty polyolefin waste has a very wide range of fractions. In addition, it contains high concentrations of heavy paraffinic hydrocarbons (with a boiling point above 300°C), which cause a relatively high melting point of the resulting product (approx. 45°C). The high content of low-boiling fraction results in a low ignition temperature of the product (approx. 30°C). In the process on an industrial scale, rapidly rising vapour undermine the solids, which are not involved in the process (sand, pollutants) and those generated during the process (the so-called fly ash). These fractions (in the previously known industrial plants) entered the condensation systems, resulting in the clogging, reducing their efficiency and adversely affected the quality of the final product. Thus formed product (particularly in the currently used systems of thermo-catalytic degradation of the polyolefins) does not meet the expectations of the market due to its high melting point, low melting point, a high degree of pollution and high cost of production.

A patent application PL372524 discloses a separator for separating a mixture of hydrocarbons in the gas phase. Hydrocarbon vapours with a temperature of 300-360°C are entered into this device. Then an inert cooling factor (e.g. nitrogen), which is meant to cool the vapour to a temperature of 280° C and condense paraffin fractions, is fed into a working chambers with vertical partitions. Condensed paraffinic fractions flow through a pipe in the bottom of the funnel-shaped working chamber to an intermediate tank, from where they are recycled to the reactor.

A Polish patent PL208902 discloses a method of fractioning a mixture of gaseous hydrocarbons, the mixture of gaseous hydrocarbons being fed to the device for fractioning a mixture of gaseous hydrocarbons, a heavy fraction is being condensed and the heavy fraction in liquid form, is fed to the light section, wherein the mixture of gaseous hydrocarbons is fed into the device for fractioning a mixture of gaseous hydrocarbons in the form of small bubbles with diameters of 2-10 mm. Patent PL208902 describes a device for fractioning a mixture of gaseous hydrocarbons having a housing, an inlet for a mixture of gaseous hydrocarbons, at least one outlet for the heavy fraction in a liquid form, and at least one outlet for the light fraction in the gaseous form, wherein at least one free edge of the inlet pipe end has a form of a serrated edge. The use of such a device is not sufficient to achieve the expected results: the stability and reliability of the system operation, specific parameters of the final products (e.g. oil fraction should have a melting point above 56°C) and process energy consumption as low as possible. To obtain the products of the desired quality and performance maintaining the lowest possible cost of conducting the process, it is necessary to carry out the fractioning in stages and in different ways for each stage.

The aim of the invention was to develop a method and a set of devices for receiving, fractioning and condensing hydrocarbon mixtures, particularly in vapour form formed during thermo-catalytic degradation of plastics, in particular the polyolefins.

A fractioning system of the invention, in contrast to the separator known from a patent application PL372524 assumes initial fractioning and separation of solid pollutants at the point of discharging vapours from the reactor (A). Obtaining a proper kinetics of this phenomenon eliminates the ingress of pollutant and tar fractions into other, more complex devices of the system. This solution also reduces the inlet vapour temperature to the first degree fractioning system (B), which improves the energy balance of the process. A fractioning system of the invention, in contrast to the separator known from a patent application PL372524 does not assume feeding any additional cooling medium into the system. Feeding such a medium (e.g. nitrogen) increases gas flow rate in a further system, which is not desirable, because of the shorter residence time of the particles in particular zones of the system, which results in worse fractioning conditions. Fed nitrogen must be discharged from the system together with the uncondensed gases with a hydrocarbon chain lengths ranging from CI to C4, which reduces the caloric content, and worsens the conditions of subsequent combustion. Said separator does not allow separating the resulting fraction ranging from C5-C18 what is necessary to get the final products such as liquid fuels, solvents or other chemicals.

The essence of the invention is a method for receiving, fractioning and condensing gas mixtures, particularly hydrocarbon formed during thermo-catalytic degradation of plastics carried out in the reactor adapted for conducting the thermo-catalytic degradation process of plastics characterized in that it is carried out under overpressure of 0 to 2 bar, wherein separation of solid particles takes place at the reception stage of the gas mixtures in the vapour discharge system while self-recycling to the reactor the fractions with a boiling point above 360°C, then the gas mixture passes to the first degree fractioning system, wherein fractions with a boiling point of 290-360°C are being separated, then the gas stream is subjected to condensation in a condensation system and the stream of hydrocarbon vapours with a boiling point below 30°C, which were not condensed, is received as one of the products of fractioning. Preferably, a fraction with a boiling point of 290-360°C is recycled to the reactor adapted for conducting the thermo-catalytic degradation process of plastics or is cooled and then stored as a product of the process in the form of technical paraffins.

Preferably, gas mixture passes through the vapour discharge system, first degree fractioning system, second degree fractioning system, then condensed oil fraction of the oil flows through oil fraction cooling system and then it is collected in an intermediate oil fraction tank and the remaining vapour stream passes through the low-boiling fraction condensation system and hydrocarbon vapours with a boiling point above 30°C are released to the intermediate low-boiling fraction tank.

Preferably, a gas mixture passes through the vapour discharge system, first degree fractioning system, second degree fractioning system, then the oil fractions are condensed in the oil fraction condensation system and collected in an intermediate oil fraction tank and the remaining vapour stream passes through the low-boiling fraction condensation system and hydrocarbon vapours with a boiling point above 30°C are released to the intermediate low-boiling fraction tank.

Preferably, a gas mixture passes through the vapour discharge system, first degree fractioning system, wide hydrocarbon fraction condensation system and then hydrocarbon vapours with a boiling point above 30°C are released to the intermediate wide hydrocarbon fraction tank.

Preferably, a gas mixture formed during the thermo-catalytic degradation of plastics passes through the vapour discharge system which comprises at least one vertical channel and at least one horizontal channel, wherein the vertical channels have the total cross-sectional area of at least 10%, and horizontal channels have the total cross- sectional area of at least 3% of the liquid surface level (weight of waste) in the reactor and are at a height of 0.5 m to 6 m above the surface.

Preferably, a gas mixture is fractioned in a first degree fractioning system, having at least one inlet pipe, at least one vapour outlet pipe, at least one paraffin outlet pipe, at least one partition wall and the bottom of the fractioning surface and the bottom wall of the interceptor located at an angle to the horizontal.

Preferably, fractioning of the gas mixture in the first degree fractioning system takes place in the volume of this system and on the partition walls, which are flat plates and/or the perforated plates and/or pipe bundles and/or open-work structures of steel profiles and/or spirals, preferably partition walls are cooled from the inside by a cooling medium.

Preferably, condensed fraction with a boiling point of 290-360°C sink to the bottom of the fractioning surface located at an angle of from 2 to 5° to the horizontal and decrease towards the intermediate paraffin tank. Another object of the invention is a set of devices used for receiving, fractioning and condensing gas mixtures, particularly hydrocarbon formed during thermo-catalytic degradation of plastics conducted in the reactor adapted for conducting the thermo- catalytic degradation process of plastics is characterized in that it comprises a vapour discharge system, first degree fractioning system and condensation system.

Preferably, the condensation system includes the second degree fractioning system and/or oil fraction cooling system and/or intermediate oil fraction tank and/or low- boiling fraction condensation system and/or intermediate low-boiling fraction tank and/or second degree fractioning system and/or oil fraction condensation system and/or hydrocarbon fraction condensation system and/or intermediate wide hydrocarbon fraction tank.

Preferably, a set of devices comprises a vapour discharge system, first degree fractioning system, second degree fractioning system, oil fraction cooling system, intermediate oil fraction tank, low-boiling fraction condensation system and intermediate low-boiling fraction tank.

Preferably, a set of devices comprises a vapour discharge system, first degree fractioning system, second degree fractioning system, oil fraction condensation system, intermediate oil fraction tank, low-boiling fraction condensation system and intermediate low-boiling fraction tank.

Preferably, a set of devices comprises a vapour discharge system, first degree fractioning system, hydrocarbon fraction condensation system and intermediate wide hydrocarbon fraction tank.

Preferably, the vapour discharge system has at least one vertical channel and at least one horizontal channel, wherein the total cross-sectional area of the vertical channels is at least 10%, and the total cross-sectional area of the horizontal channels is at least 3% of the liquid surface level (weight of waste) in the reactor and are at a height of 0.5 m to 6 m above the surface.

Preferably, a first degree fractioning system adjoins or is situated directly at the reactor, being thermally insulated.

Preferably, a first degree fractioning system has at least one inlet pipe, at least one vapour outlet pipe, at least one paraffin outlet pipe, at least one partition wall and the bottom and the bottom wall of the interceptor located at an angle to the horizontal.

Preferably, partition walls are flat plates and/or the perforated plates and/or pipe bundles and/or open-work structures of steel profiles and/or spirals.

Preferably, partition walls are cooled from the inside by a cooling medium.

Preferably, the bottom is located at an angle of from 2 to 5° to the horizontal level and decreases towards the intermediate paraffin tank. Preferably, a second degree fractioning system has at least one vapour i nlet pipe in the bottom part, at least one vapour outlet pipe, at least one outlet pipe of liquid oil fraction, at least one heat exchanger and at least one partition wall.

Preferably, the second degree fractioning system has the shape of a column with a height of 2 m and a diameter of 300 to 3000 mm.

Preferably, partition walls are inclined to the direction of vapour flow through the column and are flat plates and/or the perforated plates and/or pipe bundles and/or open-work structures of steel profiles and/or spirals.

Preferably, partition walls are cooled from the inside by a cooling medium.

Preferably, the second degree fractioning system has at least one level of random packings.

Preferably, the second degree fractioning system has at least one level of trays collecting the condensate flowing from the above layer of random packings with the outlet pipe.

Preferably, at least one partition wall is located in the second degree fractioning system above the inlet, above there is a heat exchanger, above which there is at least one level of random packings, above there is a heat exchanger located above the vapour outlet pipe.

Preferably, a low-boiling fraction condensation system is at least one shell-and-tube heat exchanger with an inside diameter of 100 to 400 mm and a length of 4 to 20 m, inclined at an angle of 2-6° to the horizontal.

Preferably, an oil fraction condensation system is at least one shell-and-tube heat exchanger

with an inside diameter of 100 to 400 mm and a length of 8 to 40 m, inclined at a n angle of 3-6° to the horizontal.

Preferably, the oil fraction condensation system are shell-and-tube heat exchangers arranged in a non-collinear manner connected in parallel and in series through plenum boxes.

Preferably, a wide hydrocarbon fraction condensation system are at least one shell- and-tube heat exchangers with an inside diameter of 100 to 400 mm and a length of 8 to 40 m, inclined at an angle of 3-6° to the horizontal.

Preferably, the wide hydrocarbon fraction condensation system are shell-and-tube heat exchangers connected in parallel through plenum boxes.

Preferably, the wide hydrocarbon fraction condensation system are non-collinear heat exchangers connected in series through plenum boxes. Preferably, intermediate product tanks: intermediate oil fraction tank, intermediate low-boiling fraction tank and intermediate wide hydrocarbon fraction tank have product inlets at ¾ of their height, liquid product outlet at the bottom and gaseous product outlet at the top.

Preferably, a second degree fractioning system has at least one inlet pipe, at least one vapour outlet pipe, at least one outlet pipe of liquid mixture and vapour oil fraction, at least one heat exchanger and at least one partition wall.

Preferably, the second degree fractioning system has the shape of a column with a height of 3m and a diameter of 300 to 3000 mm.

Preferably, the inlet pipe is located in the central part of the column.

Preferably, partition walls are arranged obliquely to the direction of vapour flow and are flat plates and/or the perforated plates and/or pipe bundles and/or open-work structures of steel profiles and/or spirals.

Preferably, partition walls are cooled from the inside by a cooling medium.

Preferably, the second degree fractioning system has at least one level of random packings.

Preferably, the second degree fractioning system has at least one level of trays collecting the condensate flowing from the above layer of random packings with the outlet pipe.

Preferably, the second degree fractioning system is cooled from the outside over the entire length.

Preferably, at least one partition wall is located in the second degree fractioning system above or below the inlet, above there is a heat exchanger, above there is at least one level of random packings, above there is a heat exchanger located above the vapour outlet pipe.

Presented method of receiving, fractioning and condensing gas mixtures, formed during thermo-catalytic degradation of polyolefins allows to eliminate key disadvantages of this process (and related processes). Due to the large amount of pollutants, high concentration of high-boiling fractions, uneven vapour efficiency and economic aspects in practice it is impossible to use the fractioning system based on prior art (for example appropriate for processing =crude oil in an industrial environment). A fractioning process of the invention is carried out under low overpressure (preferably 0 to 2 bar), therefore there is no need to provide particularly robust and expensive devices. The invention will now be further described in embodiments and was presented in the drawing, in which: fig. 1 shows the view illustrating the installation comprising a vapour discharge zone (A), first degree fractioning zone (B), second degree fractioning zone (C), oil fraction cooling zone (D), zone of intermediate receiving of oil fractions (E), low-boiling fraction condensation zone (F), zone of intermediate receiving of low boiling fractions (G); fig. 2 shows the view illustrating the installation comprising a vapour discharge zone (A), first degree fractioning zone (B), second degree fractioning zone (option 2) (K), oil fraction condensation zone (H), zone of intermediate receiving of oil fractions (E), low-boiling fraction condensation zone (F), zone of intermediate receiving of low boiling fractions (G); fig. 3 shows the view of the installation comprising a gas mixture receipt zone (A), gas mixture fractioning zone (B), wide hydrocarbon fraction condensation zone (I), wide hydrocarbon fraction intermediate receipt zone (J); fig. 4 shows an example construction of first degree gas mixture fractioning system (B); fig. 5 shows a distillation and rectification column of the second degree fractioning system (C), fig. 6 shows a distillation and rectification column of the second degree fractioning system (K), fig. 7 shows an example, alternative construction of a first degree fractioning system (B).

A method of the invention is to discharge vapours from the reactor's working chamber at a suitable height (from 0.5 m to 6 m, most preferably from lm to 3m over a liquid surface level - weight of waste in the reactor). In order to reduce the vapour flow rate, vapour discharge channels preferably have large area cross-sections: vertical channels (A 1) (as indicated in fig. 1) in total at least 10% (most preferably 15-20%), and horizontal (A 2) at least 3% (most preferably 5-6%) of the liquid surface level in the reactor. This solution results in a significant reduction of escaping from the reactor the solid fractions and hydrocarbons with a high boiling point (above 360°C) which are undesirable in the final product and could be deposited on the surfaces of further devices for receiving the product in liquid form (first degree fractioning system (B), second degree fractioning system (C), condensation system (F, H, I)), resulting in the need for their frequent and troublesome cleaning. According to the invention it is possible to discharge hydrocarbon vapours through one or many channels (A), which is an additional advantage of using the invention with the reactor of considerable size or elongated shape. Channels (A2) preferably are as short as possible and isolated.

First degree fractioning system (B) preferably adjoins or is situated directly at the reactor. Second degree fractioning system (B) is preferably thermally insulated.

Horizontal vapour discharge channels (A2) are directed to the interceptor (B 3) of the first degree fractioning system (B), which are preferably is expanded, and their flow rate decreases. The bottom wall of the interceptor (B 5) is angled relative to the horizontal (most preferably 4-7°) so as to expand the channel towards the outlet. This wall is preferably at the same time the top wall of the fractioning surface (B 6), which minimizes the heat transfer surface. Through the contact of the vapours with the walls and many partition walls (B7) in the form of flat plates, perforated flat plates or open- work partition walls (e.g. of steel profiles) vapour temperature drops and heavy paraffin fractions condensate. Inside the separator, due to a specific arrangement of the partition walls re-evaporation of the lighter fractions occurs (which has been condensed by contact with the partition walls), through their heating while in contact with encircling vapours.

Depending on the assumed composition of the exhaust vapour stream the surface of the internal partition walls can be changed. Increasing the surface of partition walls increases the concentration of less volatile fractions in the condensate formed in the separator. The concentration and the amount of fractions condensed at this stage can be controlled by changing the volume and the surface area of the outer fractioning wall (B 6) as well as isolation parameters of these walls. Intensification of heat exchange through the walls (by increasing their surface or decreasing their thermal resistance) will increase the amount of condensate and concentration of high volatility fraction. The invention implies the possibility of automatic control of the process parameters by the use of cooled partition walls (e.g. in the form of plates or spirals filled with a cooling factor) and the measurement of vapour temperature at the outlet of the system.

Condensed fractions (mainly paraffin with boiling points from approx. 290 to approx. 360°C) flow down by gravity through the sloped bottom of the fractioning surface (B 8), preferably set at an angle of 2-5° to the horizontal, into the cavity at the bottom part functioning as the intermediate paraffin tank (B 9). Via the paraffin outlet pi pe (B

1) , these fractions can be directly (with no appreciable temperature change) recycled to the reactor adapted for conducting the thermo-catalytic degradation process of polyolefins for further degradation or transported to the next cooled intermediate tank as one of the final products of the process.

Vapour outlet pipe (B 2) may be positioned at any height and at any angle to the inlet pipes (B 4), which simplifies deployment of elements of the system.

Examples of possible implementation of the device are shown in fig. 4 and fig. 7.

Fractions with a temperature of approx. 140-200°C and the boiling temperature of approx. 290°C uncondensed in the first degree fractioning system (B) through a pipe (B

2) enter further devices in which the processes are conducted using one of the following three described methods:

Example I:

Uncondensed fractions with a temperature of approx. 140-200°C enter the bottom part of the second degree fractioning system (C) through a vapour outlet pipes (B 2) and vapour inlet pipe (C 3). This system has a form of a distillation and rectification column particularly adapted for the thermo-catalytic degradation of polyolefins. The diagram of this column is shown in fig. 5. The vapours are directed towards the top, where they encounter the partition walls (C4) (in the form of flat plates, perforated flat plates or open-work partition walls which may be cooled from inside) and a heat exchanger (C 5), which are used for the condensation of the heaviest fractions and prevent them from entering the higher levels of the column, which are more sensitive to pollution. Above there is a multiple condensation and evaporation zone of the factor (C 7) divided into levels separated by open-work shelves - condensate trays (C6), collecting the condensate from the a given level. The most preferable method of realising these zones (C 7) are random packings (e.g. metal or ceramic Raschig, Biatecki, Pall or other rings), which are not as susceptible to contamination as valve, valveless shelves or structural packings and provide the opportunity to operate at changing vapour efficiency. It is possible to receive liquid intermediate products (condensate) from selected levels of trays (C 6). In the upper part of the column there is a heat exchanger (C 5) which controls the temperature and composition of the products which leave the column in the gas phase. The heat exchanger may be located along the entire length of the column in the form of a spiral within the column or a shell outside the column.

Vapours at a temperature of approx. 60-120°C enter the low-boiling fraction condensation system (F) through the upper vapour outlet pipe (C 1). The system is preferably composed of a shell-and-tube heat exchanger, inclined at an angle to the horizontal (most preferably 2-6°) with an inside diameter of 100 to 400 mm and a length of 4 to 20 m. Then the condensed fractions flow down to the intermediate low- boiling fraction tank. Uncondensed gases C1-C4 (with a boiling point below 30°C), which are directed to technological burners through the pipe (Gl), which may be used to supply energy in the form of heat to the process - e.g. thermo-catalytic degradation of polyolefins accumulate over their surface. Liquid low-boiling fractions are discharged to the storage tank through the pipe (G 2) located in the bottom part of the intermediate tank.

Liquid (mainly oil fractions) with a temperature of 100-180°C is fed to the oil fraction cooling system (D) through the bottom pipe of the column - oil fraction outlet pipe (C2). The system is preferably composed of a shell-and-tube heat exchanger, inclined at an angle to the horizontal (most preferably 2-6°) with an inside diameter of 100 to 400 mm and a length of 4 to 20 m. Then the condensed fractions (with a temperature of 20-50°C) flow down to the intermediate oil fraction tank (E). Liquid low-boiling oil fractions are discharged to the storage tank through the pipe (E 1) located in the bottom part of the intermediate tank.

Example II :

Fractions with a temperature of approx. 140-200°C uncondensed in the first degree system through a pipe (B2) and vapour inlet pipe (K 3) enter the central part of the second degree fractioning system (K). This system has a form of a distillation and rectification column particularly adapted for the thermo-catalytic degradation of polyolefins. The diagram of this column is shown in fig. 6. Vapours get into the space with a number of partition walls (K 4) (in the form of flat plates, perforated flat plates or open-work partition walls which may be cooled from inside), both above and below the inlet. Through the contact with the partition walls, some of the vapours are condensed and flow down the column. With the proper flow kinetics obtained by complex arrangement and number of partition walls a gas composition at the top and bottom of the column differs. Light low-boiling fractions flowing up the column dominate in the upper part of the column. A layer of random packings (K 7), condensate trays (K 6) and a heat exchanger (K5) which support the fraction separation and control this process. The heat exchanger may be located along the entire length of the column in the form of a spiral within the column or a shell outside the column.

So separated low-boiling fractions with a temperature of 60-120°C enter the low- boiling condensation system (F) through the vapour outlet pipe (Kl). Then condensed fractions flow down into the intermediate low-boiling fraction tank (G). Uncondensed gases C1-C4 which are directed to technological burners through the pipe (Gl), which may be used to supply energy in the form of heat to the process - e.g. thermo-catalytic degradation of polyolefins accumulate over their surface. Liquid low-boiling fractions are discharged to the storage tank through the pipe (G 2) located in the bottom part of the intermediate tank.

Liquid and vapours (mainly oil fractions) with a temperature of 100-180°C are fed to the oil fraction condensation system (H) through the bottom pipe of the column - oil fraction outlet pipe (K 2). The condensation system consists of shell-and-tube heat exchangers. Exchangers preferably have a circular cross section with diameter of 100- 400 mm. It is possible to put a couple of exchangers connected in parallel and in series. The length of the heat exchanger of the invention should be as long as possible. In practice, preferably, its length should be comprised within the range of 8-40 m. Accoring to the invention it is possible to set a series of heat exchangers in a non- collinear manner, which significantly limits the dimensions of the entire system. Non- collinear heat exchangers should be connected with each other through plenum boxes. According to the invention it is possible to connect the heat exchangers in parallel - also through plenum boxes. This arrangement prevents the pollutants from depositing in the elbows and allows for equalization of pressure inside the respective heat exchangers. The exchangers are preferably arranged obliquely to the horizontal (most preferably 3-6°), which allows free flow of condensed product and prevents depositing of possible pollutants or paraffin fractions. Then condensed fractions (with a temperature of 30-60°C) flow down into the intermediate oil fraction tank (E). Uncondensed gases C1-C4 which are directed to technological burners through the pipe (E 2), which may be used to supply energy in the form of heat to the process - e.g. thermo-catalytic degradation of polyolefins accumulate over their surface. Liquid low- boiling oil fractions are discharged to the storage tank through the pipe (E 1) located in the bottom part of the intermediate tank. Example III:

All fractions in the form of vapours enter the wide fraction condensation system (I). The condensation system consists of shell-and-tube heat exchangers. Exchangers preferably have a circular cross section with diameter of 100-400 mm. It is possible to put a couple of exchangers connected in parallel and in series. The length of the heat exchanger of the invention should be as long as possible. In practice, preferably, its length should be comprised within the range of 8-40 m. Accoring to the invention it is possible to set a series of heat exchangers in a non-collinear manner, which significantly limits the dimensions of the entire system. Non-collinear heat exchangers should be connected with each other through plenum boxes. According to the invention it is possible to connect the heat exchangers in parallel - also through plenum boxes. This arrangement prevents the pollutants from depositing in the elbows and allows for equalization of pressure inside the respective heat exchangers. The exchangers are preferably arranged obliquely to the horizontal (most preferably 3-6°), which allows free flow of condensed product and prevents depositing of possible pollutants or paraffin fractions. The product (wide hydrocarbon fraction) flows down into an intermediate tank (J), where it is received below the level of the liquid to the storage tank through the pipe (J 1). Residues of uncondensed fractions are received by a pipe (J 2) located above the level of the liquid and may be directed to technological burners which may be used to supply energy in the form of heat to the process - e.g. thermo-catalytic degradation of polyolefins.

By using the method and devices of the invention obtaining gas and oil fractions of polyolefin wastes can be faster and cheaper. Relative to the previous, more commonly known solution (in which production of oil fraction took place in two separate process lines), the average efficiency of the process was improved from approx. 1001 of oil fractions to approx. 200 l/h while maintaining a similar energy consumption of the process. It significantly reduced the number of failures. The need for cleaning of the condensation system was eliminated, which in the previous solutions forced the necessity of stopping the process for approx. 12 hours every 2.5 days.

Description of elements:

A- Vapour discharge system

A 1 - vapour discharge vertical channels

A 2 - vapour discharge horizontal channels

B- First degree fractioning system

B 1 - paraffin outlet pipe

B 2 - vapour outlet pipe

B 3 - interceptor

B 4 - vapour inlet pipe

B 5 - bottom wall of the interceptor B 6 - f ractioning surface

B 7 - partition walls

B 8 - bottom of the fractioning surface

B 9 - intermediate paraffin tank

C- Second degree fractioning system

C I - vapour outlet pipe

C 2 - liquid oil fraction outlet pipe

C 3 - vapour inlet pipe

C 4 - partition walls

C 5 - heat exchanger

C 6 - condensate trays

C 7 - random packing

D- Oil fraction cooling system

E- intermediate oil fraction tank

E 1 - oil fraction - product pipe

E 2 - uncondensed hydrocarbon C1-C4 - product pipe F- Low-boiling fraction condensation system

G- Intermediate low-boiling fraction tank

G 1 - uncondensed hydrocarbon C1-C4 - product pipe

G 2 - low-boiling fraction - product pipe

H- Oil fraction condensation system

I- Wide hydrocarbon fraction condensation system J- Intermediate wide hydrocarbon fraction tank K- Second degree fractioning system - option 2

K 1 - vapour outlet pipe

K 2 - oil fraction outlet pipe

K 3 - vapour inlet pipe

K 4 - partition walls

K 5 - heat exchanger

K 6 - condensate trays

K 7 - random packing