EA006452B1 - A compact rectifying unit for separation of mixed fluids and rectifying process for separation of such mixed fluids - Google Patents

Abstract

The invention relates to a compact rectifying unit for separation of mixed fluids using for heat transfer purpose a fluid heat carrier and its vapours on one of the sides of heat and mass exchanging walls. In order to increase the efficiency of the heat and mass exchange process, the heat and mass exchange tubes of the rectifying part and/or of the evaporator part have means to provide irregular (varying) amounts of heat transfer between the inside and the outside of tube wall along the height of said heat and mass exchange tubes. This allows to reduce the rectification column height by 3-10 times.

Description

The invention relates to a compact distillation unit for separating mixed fluids in accordance with the restrictive part of claim 1, a compact evaporator unit for a distillation unit in accordance with the restrictive part of claim 33 of the claims, as well as to a distillation method for separating mixed fluids in accordance with the restrictive part of clause 34 of the claims.

The operation of the traditional distillation column, including the film column, is that the flow of moist reflux obtained in a reflux condenser outside the zone of heat and mass transfer between water vapor and liquid is transferred to the top of the column. Thus, the flow C of vapor and the flow B of liquid reflux are constant at all levels of the height of the column. The flow of liquid reflux b is usually much more intense than the flow of flow P when sampling distillate (see Fig. 1).

In the film column, like the one proposed, the flow L of liquid reflux is formed directly at all levels of the height of the heat and mass transfer zone. This liquid reflux stream is produced by creating a temperature gradient through the heat exchange wall at each level of the column height, and it flows down the heat exchange wall as a thin film. Thus, conditions are created for the forced condensation of C1 vapors at a height of 111 in the idealized separation cascade. During the condensation of the C1 vapor at this point, a simultaneous formation of a stream of liquid liquid phlegm, enriched with nonvolatile components of the mixture, and the formation of a secondary stream of C2 vapor enriched with light components of the mixture occurs (see Fig. 2). This process is repeated along the height of the column until the required concentration of distillate on the light components of the initial mixture is reached.

The objective of the invention is to improve the efficiency of the process of heat and mass transfer. This problem is solved using a compact distillation unit with features according to claim 1 of the claims and using a compact evaporation unit according to features according to claim 33. And, finally, the problem is solved using the method according to the features of clause 34 of the claims.

In accordance with the invention, an irregular temperature gradient between both sides of the wall of the heat exchange tube is provided along the height of the column. Thus, there is an irregular transfer of thermal energy through the wall of the heat exchange tube and / or between the vapor phase and the liquid phase on at least one side of the wall of the heat exchange tube, one of the possible sequences may be the irregular formation of reflux flow along the height of the column, which is consistent with the properties of distilled fluid.

Excess heat generated during the formation of liquid reflux is discharged through the wall of heat and mass transfer surface with an excess of heat accumulation by means of external boiling heat carrier, which is enclosed inside the space on the opposite side of the wall of heat and mass transfer surface.

The present invention allows to obtain low values of the height of the idealized separation cascade in a film column at high loads of the vapor flow column, and these loads are comparable to the loads for packed industrial distillation columns. In practical applications, this allows reducing the height of the distillation column by 3-10 times and reducing the content of separating materials in the column by 50-100 times as compared with conventional distillation columns.

It should be noted that the heat transfer through the walls of the heat and mass transfer tubes can vary widely over the height of the column and heat and mass transfer tubes, respectively. Although it is preferable to vaporize or condense the components of the mixed fluids in the inner space of heat and mass transfer tubes and ensure the presence of a heat transfer fluid in the annular annular space around the heat and mass transfer tubes, within the scope of the claims of the invention, it is in principle possible to evaporate and / or condense the mixed fluid the medium in the space outside the heat and mass transfer pipes and pass the fluid medium through the inner space of the pipe.

It is also important to mention that for the purposes pursued by the invention, heat exchange occurs not only between both sides of the walls of heat and mass transfer pipes. Heat transfer can also occur between the mixed components and / or between the vapor phase and the liquid phase of the mixed fluids.

Finally, it is important to mention that the mass transfer of the components of mixed fluids can occur within the steam central flow, i.e. at some distance from the surfaces of the walls of heat and mass transfer pipes, and / or mass transfer between the components of the mixed fluids can occur between the vapor phase and the liquid lightly mobile fluid on the surface of the walls of the heat and mass transfer pipes.

One of the specific advantages of this invention is that it provides highly efficient rectification of mixed fluids in a very wide, almost unlimited range. In particular, the correlation between the boiling points and the condensation energy and evaporation of the components of the mixed fluids that are to be separated is optional. AT

- 1 006452 in particular, the use of a heat-transfer fluid, which itself is a mixed fluid making transitions between the vapor and liquid phases, provides a very effective means of changing heat transfer between both sides of the walls of heat and mass transfer pipes in a very wide range along the height of and mass transfer pipes. Although the temperature of the walls of the heat and mass transfer tubes may be constant along their height, this temperature will preferably vary widely over the height of the heat and mass transfer tubes to support the formation of an irregular heat transfer profile along the height of the heat and mass transfer tubes. In addition, the formation of a specific profile of phlegm along the height of the heat and mass transfer tubes, in which the reflux is preferably irregular, i.e. not constant along the height of the heat and mass transfer pipes, will stabilize the equilibrium between the vapors and the liquid at each stage of distillation (distillation), i.e. at various height levels of heat and mass transfer pipe.

Brief Description of the Drawings

FIG. 3 shows the formation of an irregular flow b of liquid reflux for the distillation part 12 of the column 10 due to irregular heat transfer along the height H of the heat and mass transfer pipe 2 with a decreasing (bottom to top) temperature gradient.

FIG. 4 shows the formation of an irregular flow of liquid reflux for the evaporation part 14 of the column 1 0 due to irregular heat transfer along the height H of the heat and mass exchange pipe 2 with a uniformly increasing (bottom to top) temperature gradient.

FIG. 5 shows the formation of an irregular flow b of liquid reflux for the rectifying part 1 2 of the column 1 0 due to irregular heat transfer along the height H of the heat and mass exchange pipe 2 with an unevenly decreasing (bottom to top) temperature gradient.

FIG. 6 shows the formation of another irregular flow L of liquid reflux for the evaporation part 1 4 of the column 1 0 due to irregular heat transfer along the height H of the heat and mass transfer pipe 2 with an unevenly increasing (bottom to top) temperature gradient.

FIG. 7 shows the design of the distillation column 10, providing irregular heat transfer and the formation of an irregular reflux flow along the height of the heat and mass exchange pipe 2.

FIG. 8 - the design of the second variant of the column (rectification part).

FIG. 9, 9a - the design of the third variant of the column (distillation part).

FIG. 1 0 - several examples of irregular profiles of ribs located along the outer surface of heat and mass transfer tubes.

FIG. 11 - the design of the fourth version of the column (rectification part).

FIG. 12 - the design of the fifth version of the column (rectification part).

FIG. 1 3 - the sixth alternative column (rectification part).

FIG. 14 is a flow chart of a column constructed on the basis of the above described structures of a film column.

FIG. 14a shows the scheme of the column for the distillation (distillation) of the gas condensate of the Verkh-Tatar deposit in Western Siberia.

FIG. 15 shows variants of the design of the distillation column 8 (type I, Fig. 14, 14a).

FIG. 1 6 - evaporator for the columns depicted in FIG. 1 4, 1 4a.

FIG. 1 7 is a variant of the design of the evaporator, characterized by the introduction of partitions 408 with a perforated cross section into the vapor space.

FIG. 1 8 is a flow chart of a column that has no performance limitations.

FIG. 1 9 shows the design of a film evaporator evaporator.

FIG. 20 is another embodiment of a film evaporator.

FIG. 21 - the third version of the film evaporator evaporator.

Detailed description of the drawings

In accordance with FIG. 7, the column 1 0 consists of a body 1 with plates 3 and 4 pipes, between which heat and mass transfer pipes 2 are fixed. At the bottom of the distillation part 12 of the column 10 there is a fitting 7 (inlet and outlet) for supplying coolant and fitting 6 (inlet ) to return the condensate coolant. At the top of the column there is a mouthpiece 5 (inlet and outlet) for the release of the vapor phase coolant and to return the condensate coolant.

The column works as follows. Through the nozzle 7 annular annular space 100 columns fill the coolant. The coolant for the distillation part 1 2 (section of the column) can be any mixed fluid with a boiling point in the range of the boiling point of the initial mixture, i.e. rectified mixture, to a temperature (T _B1 ) boiling it below boiling distillate. The coolant for the evaporation part (section of the column), which is discussed below, can be any liquid or mixed fluid with a boiling point in the range from the boiling point of the initial mixture to the boiling temperature (T _B2 ) of the above-boiling residue component.

The heat carrier boils under the action of heat of condensation of vapors of the distilled liquid,

- 2 006452 and condensation takes place on the inner surfaces of the walls of heat and mass transfer pipes 2 or excess heat supplied from an external source through the housing 1. Heat carrier vapors rise through the annular annular space 100 and are distributed through a fitting or mouthpiece 5 leading to the return condenser ( not shown in the drawing). From the return condenser, the distillate coolant is returned to the annular annular space of the column through a fitting or mouthpiece 5, and / or through a fitting or fitting 6. This is how to prevent leakage of coolant from the column. The temperature gradient is provided at different heights of heat and mass transfer pipes 2 with regulation of the level of boiling heat carrier in the column by means of fitting or fitting 7. Thus, both the gradient with an excess of the difference in boiling temperatures in the vapor and liquid phases, and their distribution along the height of the heat and mass transfer pipes 2.

On the inner surfaces of the walls of the tubes, a stream of liquid reflux is formed, as indicated in the above description. Reflux flows from the pipe walls in the form of a thin film. The vapor of distilled liquid rises upward through pipes 2. Along the height of pipes 2, there is a process of heat and mass transfer between the rising steam flow and the film of liquid reflux flowing down. On top of the pipes 2 comes the clean vapor phase of the distillate liquid, which is produced for condensation and cooling. At the bottom of the heat and mass transfer pipes 2, a stream of liquid reflux is withdrawn from the column, and it is either output as the target fraction, or fed to the downstream section or to the evaporation part of the column.

For additional control of the temperature gradient, the return condenser can be equipped with a pressure regulator (not shown in the drawing), and the technical means used for this are known in the industry. Increasing or decreasing the pressure in the annular annular space 100 changes both the boiling point of the heat transfer medium and the temperature gradient between the vapor and the heat transfer fluid.

The alternate column design shown in FIG. 8 is similar to the construction described above in connection with FIG. 7. It differs, firstly, in the upper part of the tube space: there is a distribution plate under the zone of the condensate vapor outlet of the heat carrier 8. Secondly, the heat and mass transfer tubes 2 have a variable wall thickness along its height. In each particular case, the change in wall thickness is determined by the desired profile of liquid reflux formation, as was shown as an example in FIG. 3, 4, 5, or 6. For example, in FIG. 8 shows the variant with the wall thickness of the heat and mass transfer pipe 2, increasing at the lower end.

The column works as follows. Pairs of boiling coolant rise through the annular annular space 1 00 and are outputted through fitting 5 to the return condenser, as described above. The distillate condensate is returned through the fitting 5 and falls on the distribution plate 8. Thus, the condensate begins to be heated by the counter-current steam in the connecting pipe 5 and on the plate 8. The condensate layer 9 flows through the gaps between the bottom of the distribution plate 8 and the pipes 2 and flows down through the outer surface of the pipe 2 in the form of a thin film. The condensate film flowing downwards is also heated by the upward flow of steam coolant. Being irregular along the height of the column, the thermal conductivity of the walls of heat and mass transfer pipes 2 creates a temperature gradient. And again (horizontal) temperature gradient is achieved, as described in the previous version. Part of the condensate coolant can also be returned through the fitting or fitting 6. Heat and mass transfer with the internal space of the pipes 2 in the column is similar to the above option.

A specific embodiment, corresponding to FIG. 9 and 9a, differs from the previous one in that the heat and mass transfer tubes 2 have a constant wall thickness along the height. And on the outer surface of these pipes 2 there are fins 15 having a variable cross section along their height. The temperature gradient for this variant is achieved due to the thermal conductivity gradient due to the irregular profile of the ribs along their height. FIG. 1 0 shows a few examples of irregular edge profiles

a) rib width increases downwards;

b) rib width decreases downwards;

c) rib width decreases towards the middle;

b) the width of the rib increases unevenly downwards;

e) the width of the rib is unevenly decreasing downwards;

ί) the thermal conductivity of the rib varies unevenly with height due to the different width and depth of the grooves;

e) the thermal conductivity of the rib varies unevenly with height due to holes of different diameters unevenly located on the surface of the rib. The operation of the column is similar to the above options.

The fourth option, corresponding to FIG. 11 differs from the previous one in that instead of ribs, external pipes 1 6A are used to achieve an irregular temperature gradient, installed coaxially at some distance relative to the heat and mass exchange pipes 2. The pipes 1 6A installed in this way are perforated with holes 11, the number of which is unevenly distributed

- 3 006452 leno pipe height. The irregularity of the temperature gradient along the height of the heat and mass transfer pipes 2 is achieved by the conditions of irregular heat transfer by convection along the height of these pipes supported on the outer surface of the heat and mass exchange pipes. For example, in FIG. 11 shows a variant with an increase in the degree of perforation from top to bottom. The operation of the column is similar to the above options.

The fifth option, corresponding to FIG. 12 differs from the previous one in that the heat and mass transfer pipes 2 are surrounded by coaxially mounted pipes 16B located at some distance from them and having irregular internal cross sections (flow sections) along their heights. In the lower and upper parts of the pipes 16B there are holes 11 for the entry of the coolant into the heat and mass transfer pipes 2 and for removing its vapor from above. The irregularity of the temperature gradient along the height of heat and mass transfer pipes 2 is achieved by establishing the conditions for irregular heat transfer by convection from the outer surface of the pipes 2 along their height. This irregularity is achieved (in particular) due to the gradient of the velocity of the coolant vapor flowing around the surface of the pipes 2 in the changing gap with the pipes 1 6B. For example, in FIG. 1 2 shows a variant with a decrease in the flow area from top to bottom. The operation of the column is similar to the above options.

The sixth option, corresponding to FIG. 13 is similar to the structure shown in FIG. 8, and differs from it in that the boiling coolant provides the use of an external chamber 611. The level of the coolant is preferably lower than the plate 4 of the pipes. The coolant in the chamber 611 boils due to the supply of heat through the walls of the chamber from an external heat source (not shown in the drawing), for example through a shirt. The chamber 611 is connected to the plate 4 pipes through a fitting or fitting 6, and, in addition, to the bottom of the housing 1 by means of a connecting pipe 610. The pipe 4 plate has a channel 7B for the passage of coolant condensate. The coolant vapor passes into the annular annular space 100 of the column through the connecting pipe or fitting 6, and the return of the coolant condensate to the chamber occurs through channel 7B and the connecting pipe 61 0. The operation of the column is similar to the above options. The wall thickness of pipe 2 decreases from bottom to top, similar to that shown in FIG. eight.

You can also create variants that combine the presence of irregular wall thickness of heat and mass transfer tubes 2, irregular ribs, unevenly perforated outer casings and / or outer casings of variable cross section.

Turning now to FIG. 14, it should be noted that the distillation column according to this invention consists of the following main components: preheater 302, preheater 304, evaporator 306, combustion chamber 307, distillation column 309, condenser 310, separator 311 and return condenser 326.

Example 1. Distillation of oil obtained from the Verkh-Tatarskoe field, Western Siberia

The column works as follows. Oil is prepared in advance for distillation using standard technology. Crude oil is pumped out of the tanks at a consumption of 1250 kg / h and along the line 301 moves to the annular annular space of the heater 302, consisting of a casing and pipes. The temperature of crude oil is 10 ° C. From the column 308, through line 313, diesel fuel at a temperature of 250 ° C is supplied to the tube space of the heater 302. Cooling rapidly to a temperature of 50 ° C, diesel fuel again heats the crude oil to a temperature of 60 ° C. The vapor phase of the heated oil, including natural non-condensable gas, is discharged directly into the condenser 310 on top of the preheater 302 via line 317. There is another possible option, i.e. the flow of oil into the tubular space of the heater 302 and the supply of diesel fuel into the annular annular space of the heater 302.

The fluid phase of the heated oil is supplied to the annular annular space of the heater 304, consisting of a housing and pipes, via line 303. The oil residue at a temperature of 360 ° C is fed into the pipe space of the heater 304 from the evaporator of evaporator 306 through line 315. Cooling rapidly to a temperature of 95 ° C, the oil residue in the reverse flow heats the crude oil to a temperature of 129 ° C. It is also possible to feed crude oil into the tube space of the preheater 304, and the oil residue into the annular annular space.

The heated oil passes into the annular annular space 341 of the initial part of the evaporator 306 through line 305. In the evaporator, the oil is heated by hot combustion gases coming in a reverse (counter-current) flow from the furnace chamber 307 through the heating tubes 340. In the final part of the evaporator 306, the oil is heated up to 360 ° C. The oil supply is controlled by the heating temperature in the final part of the evaporator 306, which is also the evaporator part of the column 308. The light hydrocarbon vapors from the evaporator 306 enter the column 308. The oil residue fraction, which heated to 360 ° C through the evaporator part of the evaporator 306, is discharged into 304 heater for cooling. From the evaporator, flue gases are released via line 321 to chimney 337.

In the column 308 with heat and mass transfer tubes 350, a process of heat and mass transfer occurs, as a result of which the vapors of light hydrocarbons are separated into the fluid phase of the diesel fuel fraction and the vapor phase of the gasoline fraction. The height of the heat and mass transfer part of the column 308 is

- 4 006452 em 1.5 m. Diesel fuel is discharged from the column through slit plate 320 in the temperature range 220-270 ° C and supplied for cooling to the heater 302. Pairs of gasoline fraction having a temperature range of 110-120 ° C are fed to the condenser 310. In the annular annular space 100 of the column 308, the coolant boils, ensuring high efficiency of the heat and mass transfer process pipes, as described earlier (in connection with Figs. 7-13). As a heat carrier, for example, a mixture of high-quality alcohol with water is used. In the jacket 323 at the bottom of the column 308, through line 322, part of the flue gases is fed from line 321, which transfer their heat to the coolant in the annular annular space 100. The amount of additional heat supplied is controlled by the damper 342. Then the flue gases are discharged from the jacket 323 through lines 324 and 341 to the exhaust pipe 337. At the top of the annular annular space 100, coolant pairs along line 324 are diverted to return capacitor 326. The coolant condensate is returned back to the column via line 326 and / or via line 327. Line 327 can be partially or completely shut off by means of valve 328. The heat carrier in column 308 is regulated by supplying it to tank 338 via line 339 or withdrawing from this tank through this line . The return capacitor 326 is interconnected with the atmosphere through a pressure regulator 343. This regulator 343 provides a constant pressure at atmospheric or elevated pressure in the annular annular space 100. When the pressure changes, the regulator 343 provides a change in the temperature of the coolant in the column 308.

The vapor of the gasoline fraction on top of the column 308 is fed through line 309 to the condenser 310. Here, the gasoline fraction condenses and cools to 30-50 ° C. The cooled gasoline from the condenser 310 enters the separator 311.

Separator 311 separates natural gas and water condensate from a previously obtained gasoline fraction. From the bottom of the separator 311, water condensate is discharged via line 334 to the furnace chamber 307 at a consumption of 3 kg / h. In the furnace chamber, the gas condensate passes through a coil 335. Here, condensate water is released and supplied as steam to the furnace chamber to neutralize the burning of residual hydrocarbon, which remains in the original condensate water. Natural gas at the top of the separator 311 is fed via line 329 through the fire-resistant device 330 in the burner 331 for liquefaction into the furnace chamber 307. Natural gas consumption is 48 kg / h. Gasoline, freed from water and gas, is pumped from separator 311 through line 312 to tanks with a consumption of 414 kg / h.

The cooled diesel fuel from heater 302 is pumped through lines 314 to tanks at a consumption of 454 kg / h. The cooled oil residue is pumped out of the heater 304 into tanks with a consumption of 331 kg / h.

Chamber 307 of the furnace has a lighting burner 332 and a gas burner 331, for which natural gas is used. Igniting the burner is designed to start the column in operation and can be turned off during further work. FIG. 14 shows a variant of operation on diesel fuel, which is obtained from the column via line 333. In addition, the furnace chamber can be equipped with an emergency burner (not shown in the drawing), which ensures the reliability of the process of burning natural gas. The flue gases from the combustion chamber are fed to the heating tubes of the evaporator 306 for heating and evaporating the oil. Part of the flue gases with excess heat is removed through the exhaust pipe 337. The amount of flue gases required for operation of the evaporator is controlled by the valve 336. The residual heat of the flue gases removed from the column can be recovered by methods known in the industry.

Example 2. Distillation of gas condensate obtained from the Verkh-Tatarskoye field, Western Siberia

The column layout corresponds to FIG. 14a, and the column operates as follows. The condensate from the reservoir (not shown in Fig. 14a) is pumped out at a consumption of 1000 kg / h via line 301 to the annular annular space of the heater 302, consisting of a housing and pipes. Furnace fuel at a temperature of 220-240 ° C is fed into the tube space of heater 302 from evaporator 306 via line 315. Cooling rapidly to 40 ° C, the furnace fuel heats the condensate in reverse flow to a temperature of 31 ° C. The vapor phase of the heated gas condensate, including natural non-condensable gas, is discharged directly from above the heater 302 via line 317 to the condenser 310. Gas condensate can also be supplied to the tube space of the heater 302 and the fuel supply to the annular annular space.

The heated gas condensate enters via the line 305 to the annular annular space 341 of the initial part of the evaporator 306. In this evaporator, the condensate is heated by hot gaseous combustion products flowing in the reverse flow from the furnace chamber 307 through the heating tubes 340. In the final part of the evaporator 306, the condensate is heated to 220-240 ° s Regulation of the gas condensate supply is carried out by the heating temperature in the final part of the evaporator 306, which is also the evaporator part of the column 308. The light hydrocarbon vapors from the evaporator 306 enter the column 308, and the fuel fuel fraction, which is heated to 220-240 ° C by the evaporator part of the evaporator 306 , is diverted to preheater 304 for cooling. From the evaporator, flue gases are released via line 321 to chimney 337.

In the column 308 in the heat and mass transfer pipes 2, the process of heat and mass transfer takes place, in re

- 5 006452 as a result of which light hydrocarbon vapors are separated into a fluid phase, light fractions of diesel fuel and a vapor phase of a gasoline fraction. The height of the heat and mass transfer part of the column is 1.5 m. The light fraction of diesel fuel returns to the evaporator 306 and is discharged from it as a structure of the fuel fuel fraction through line 315 to the heater 302 for subsequent cooling, and the gasoline vapor fractions having a temperature of 105- 115 ° C, are fed to the condenser 310. Column 308 works in the same way as described above. The vapor of the gasoline fraction on top of the column 308 is fed through line 309 to the condenser 310. Here, the gasoline fraction condenses and cools to 30-50 ° C. The cooled gasoline from the condenser 310 enters the separator 311.

The separator separates natural gas and water condensate from the previously obtained gasoline fraction. From the bottom of the separator 311, water condensate is discharged via line 334 to the furnace chamber 307 at a consumption of 2.5 kg / h. Condensate gas passes through the coil 335 into the firebox chambers. Here, water condensate is released and supplied as vapor to the smoke cavity to neutralize the burning of hydrocarbon residues that remain in the original water condensate. Natural gas on top of the separator 311 is supplied via line 329 through the fire-resistant device 330 in the burner 331 for combustion in the furnace chamber 307. Natural gas consumption is 58 kg / h. Gasoline, freed from water and gas, is pumped out of the separator 311 through line 312 to tanks at a consumption of 826.5 kg / h.

The cooled diesel fuel from heater 302 is pumped through lines 314 to tanks at a consumption of 1 03 kg / h.

The firebox chamber 307 operates as described above.

FIG. 15 shows variants of the design of the distillation column 308 (type I, Fig. 14, 14a), while

a) to create the greatest temperature gradient along the height, the distillation column may consist of two or more sections, each of which contains a heat carrier with a different boiling point;

b) to select intermediate fractions, the distillation column may consist of two or more sections, each of which has plates for withdrawing the fraction in the lower part;

c) in order to create the most effective conditions for the rectification process, the total flow area of the heat and mass transfer tubes in each subsequent section of the column is reduced in proportion to the flows of the vapor and fluid phases in the column.

The evaporator for the column shown in FIG. 14, 14a, is a heat exchanger consisting of a body and pipes (see Fig. 16). At the ends of the housing 401 there are plates 402 and 403 of pipes in which heating pipes 404 are fixed. These heating pipes are arranged in such a way that there is a reserve annular space at the top of the housing 401. At the edge of the evaporator, next to the pipe plate 402, there is a neck 405 intended to be connected to a distillation column. A fitting 407 is located at the bottom of the housing 401 near the plate 402 for removal of the evaporation residue. On the opposite side, near the plate 403, there is a supply pipe 406 for supplying the starting material to the evaporator. This fitting 406 can be installed both at the base of the housing 401 and in the layer at the “vapor-liquid” interface of the substance (not shown in the drawing). The evaporator works as follows. The source material, such as oil, is fed into the evaporator through the supply pipe 406 and fills the annular annular space, covering the heating tubes. At the top of the evaporator there is space for permeable vapor. In the case where unheated source material is fed to the evaporator, this feed nipple is located at the base. In the case of supplying a heated starting material that supports the vapor phase, the supply nozzle 406 is in the layer at the “vapor-liquid” interface of the substance. Oil passes through the heating pipes 404 towards the neck 405. Hot flue gases flow from the combustion chamber chamber (not shown in Fig. 16), passing in the opposite direction through the heating pipes and then draining from the opposite side of the evaporator to the collector of the exhaust pipe (not shown in Fig. 16). Thus, in the evaporator heat exchange will be carried out by reverse flow (countercurrent) between oil and flue gases. As the oil gradually heats up as it moves, light hydrocarbons are released from it. At the end (on the right side according to FIG. 16) of the evaporator, the oil is heated to the maximum temperature of the fraction to be separated, so that in the area of the pipe plate 402 only the oil residue remains in liquid form. Thus, the final part of the evaporator at the same time is the evaporation part of the column. After that, the oil residue is immediately released from the evaporator to the fitting 407. The residence time of the oil at the maximum temperature does not exceed several minutes, so that the formation of carbon on the surface of the heating tubes 404 is excluded. A gradual change and a uniform increase in the boiling point of oil contributes to the effective release of light hydrocarbon fractions. The vapors of the light hydrocarbon fractions evaporated from the oil at the beginning of the evaporation process move in parallel through the free space of the evaporator towards the surface of the oil in this column. Thus, on their way, they encounter pairs of high-boiling fractions. As a result of the interaction of the vapor, the vapor phase is extracted. At the end of the evaporator, the vapors rise to the neck 405, and then flow through it into the distillation column.

FIG. 17 shows a variant of the design of the evaporator, characterized by the introduction of partitions 408 with

- 6 006452 perforated cross section into the vapor space.

These partitions, in particular, are immersed in a fluidized bed of oil. Vapors of hydrocarbons released from oil pass through perforated partitions and become turbulized. The passage of hydrocarbon vapors through perforated partitions improves the efficiency of evaporation on their surface and in the space between them.

The amount of heated oil in the evaporator is not critical. For example, the technological volume determining the evaporator capacity for a column with a capacity of 10,000 tons per year is 400 liters of oil. Since the hydrocarbon content in the evaporator and the film column is not critical, it is possible to combine the column, the evaporator and the combustion chamber in a single compact separate unit, without violating the fire and explosion safety standards.

The design of the column proposed in FIG. 14, 14a, allows you to create high-tech compact distillation systems with a yield of 100-150 tons per year based on the processed source material.

FIG. 18 shows a flow chart of a column that has no performance limitations. A distinctive feature of this column is a film evaporator evaporator 306a. The heated oil is fed through line 305 at the top of the evaporator 306A and flows downwards in the form of a thin film along the inner walls of the heating tubes 340a. The flue gases from the furnace 307 are fed into the annular annular space 341a through distribution manifold 344 and discharged from the evaporator via line 321. Flowing down, the film heats up. From it fractions of light hydrocarbons are released, which enter the distillation column 308. The remaining fraction of oil residue in the liquid state flows into the evaporation part and is discharged through line 315 to the preheater 304. The evaporator part of the evaporator has a heating jacket 347. Part of the flue gases is discharged from the cavity 307 of the furnace through line 345 to the heating jacket 347. The flue gases pass through the jacket 347 and are discharged through line 345a. The temperature in the evaporating part is regulated by the gas consumption with the help of the valve 348. Below is a detailed description of the design and operation of the evaporator. With the exception of this information, the column works in the same way as described above (see Fig. 14).

The use of a film evaporator allows to reduce the content of heated oil in comparison with the previous version of the evaporator (see Fig. 16) by 50-100 times. In combination with a film column, it is possible to combine the column, the evaporator and the firebox chamber into a single compact separate unit, without violating the fire and explosion safety standards.

The design of the column proposed in FIG. 19, allows you to create high-tech compact distillation complexes for the processing of any source material (oil, gas condensate or mixtures thereof, or other liquid mixtures) without performance restrictions.

FIG. 1 9 shows the design of a film evaporator evaporator.

This evaporator consists of a vertical casing 1 with plates 503 and 504 of pipes, between which heating pipes 2 are fixed. At the bottom of the casing 1 there is a distribution collector 506 with windows 507. The collection 506 has a connecting pipe 505 for introducing flue gases. Above the windows 507 there is a lower partition 509 with openings 508 and coaxial heating pipes 2. At the top of the housing 1 is a collector 506a with windows 507a. Collector 506a has a connecting pipe 510 for flue gas exhaust. Below the windows 507a, an upper partition 509a with holes 508a and coaxial heating pipes 2 are installed. An adapter 511 is attached to the tube plate 503 for connection to the distillation column on top of the pipe plate 503. The adapter 511 has a pipe fitting 512 for supplying the source material and a baffle 513. A bottom 514 with a jacket 516 is connected to the bottom plate of pipes 504. At the base of the cube there is a pipe fitting 515 for draining the evaporation residue. Shirt 516 has a pipe fitting 517 for flue gas inlet and pipe fitting 518 for their withdrawal.

The evaporator works as follows. The source material, such as oil, is fed to the evaporator through pipe fitting 512 and falls onto the surface of the plate 503. Deflector 513 ensures the distribution of oil over this surface. Oil in the form of a thin film flows down the inner surface of the heating pipes 2. The flue gases from the fire chamber through the connecting pipe 505 are fed into the collector 506 and are evenly distributed through the windows 507 in the shell annular space of the housing 1. Due to the presence of holes 508, the flue gases pass through the partition 509 for heating the outer surface of the heating pipes 2. Holes 508 provide uniform movement of flue gases along the heating pipes 2. This leads to a uniform vertical temperature gradient along the height of the evaporator. Due to the presence of holes 508a and windows 507a, cooled flue gases are discharged from the annular annular space of the housing 1 to the collector 506a. Then they are discharged through the connecting pipe 510. As a result of the heat exchange by the reverse flow (countercurrent), the oil film is heated and the light hydrocarbon fractions are released from it. Hydrocarbon vapors rise through pipe 2 and interact with the flowing film of liquid. As a result, heat and mass transfer takes place between them. Evaporation of oil occurs. Hydrocarbon vapors, purified from the higher-boiling fractions, leave the top of the heating tubes. From adapter 511, these pairs enter the distillation column. Bottom heating

- 7 006452 pipes 2, the oil film is heated to the maximum temperature of the separated fractions, when only the oil residue remains in the liquid phase. The film flows into a cube 514, from which a fraction of oil residue is discharged through pipe fitting 515. Part of the flue gases is fed into the jacket 516 through pipe fitting 517 to heat the cube 514. From this shirt, flue gases are discharged through pipe fitting 518.

The supply of oil and flue gases is carried out in such a way that at the bottom of the heating tubes the film is heated to the maximum temperature of the separated fractions. The heating temperature is monitored by the temperature of the oil residue in the cube. The residence time of oil in the evaporator at a critical temperature does not exceed one minute.

FIG. 20 shows another embodiment of a film evaporator.

Its construction and operation are similar to those described above. In the area of the input of flue gases from the distribution collector 506 heating pipes 2 are surrounded by coaxial sleeves 519, located at some distance from each other. Therefore, between the heating pipes 2 and the sleeves 519 there is an annular gap. The sleeves 519 protect the bottom of the heating pipes from hot flue gases, which helps to prevent the danger of burn-in of the oil residue film on the inner surfaces of the lower part of the pipes 2. The heating pipes 2 between the partitions 509 and 509a are located inside the coaxially installed restrictive pipes 520, which provides increased heat transfer efficiency from flue gas gases to the surface of the heating pipes 2. To further improve the efficiency of heat transfer, heating pipes 2 may have a vertical or horizon cial ribbing (not shown in the drawing).

FIG. 21 shows a third embodiment of a film evaporator evaporator.

Its construction and operation are similar to those described above. The annular gap between the sleeves 519 and the heating pipes 2 is filled with insulating material or liquefying substance 521 with a boiling point not exceeding the decomposition temperature in the range from the decomposition temperature of the initial mixture to the decomposition temperature of the evaporation residue. In the event of a sharp jump in the consumption and temperature of the flue gases, the fusible substance in the gap begins to melt. Within the melting time of the alloy, the temperature at the bottom of the pipes is stabilized, which provides protection against burning of the oil residue film during the controlled process time. Directly below the bottom plate 504, there is an additional plate 522. A film of oil residue flows into this plate, and then pours over its edge to the bottom of the cube 514. By introducing this plate, it is possible to further control the maximum heating temperature.

The list of positions of the drawings body heat and mass transfer pipes plates of pipes plates of pipes mouthpiece fitting union

7V channel distribution plate a layer of condensate rib holes

2 rectification part

3 column

4 rib evaporation part

And external pipes

6V inner tubes

I 00 annular space

110 column

112 rectification part

II 4 evaporation part

114A heat and mass transfer pipes

301 line

302 heater

303 line

304 heater

305 line

306 evaporator

306A film evaporator evaporator

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307 fire chamber

308 distillation column

310 capacitor

311 separators

312 line

313 line

314 line

315 line

316 line

317 line

320 crevice plate

321 lines

322 line

323 shirt

324 line

325 line

326 return capacitor

327 line

328 valve

329 line

330 fire resistant device

331 burner

332 ignition burner

333 line

334 line

335 serpentine

336 flap

337 exhaust pipe

338 tank

339 line

340 heating pipes

340a heating pipes

341 annular annular space

341A annular annular space

342 dampers

343 pressure regulator

344 distribution collection

345 line

345 A line

346 flap

347 heating shirt

348 flap

401 building

402 stove pipe

403 stove pipe

404 heating pipes

405 neck

406 supply nipple

407 fitting

408 partitions with perforated cross section

503 stove pipe

504 stove pipe

505 connecting nipple

506 collection

506A collection

507 windows

507A windows

508 holes

508A holes

509 lower partition

510 upper bulkhead

511 adapter

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512 pipe fitting

513 deflector

514 cube

5 pipe fitting

516 shirt

517 pipe fitting

518 pipe fitting

519 coaxial bushes

520 coaxial limiting tubes

521 heat insulation material

522 plate

610 connecting nipple

611 inner chamber C vapor flow

111 separation height

B liquid reflux stream

P sampling distillate

Claims (34)

1. A compact distillation unit for separating mixed fluids, including a distillation tower or column containing a) the outer casing b) means for outputting the vapor phase on top of the tower or column, c) means for withdrawing the liquid phase from below the tower or column, d) tube sheets or slabs between which at least one heat and mass transfer pipe of a tower or column is fixed, and tube sheets support heat and mass transfer pipes inside the outer casing, e) means for evaporating the mixed fluid, having means for heating the mixed fluid, the inner space of the heat and mass transfer tubes or heat and mass transfer tubes being in fluid communication with the means for evaporation, wherein the tube sheets or plates, heat and the mass transfer pipe or heat and mass transfer pipes and the casing limit the annular annular space between the casing and the pipe or pipes, while the tube sheets or plates, heat and mass transfer pipes and the casing are filled we teach the heat carrier and its vapors and are connected with a return condenser and with a means for heating the heat carrier, characterized in that the distillation column has means for providing a variable degree of heat transfer between the spaces inside and outside the pipe wall along the height of the heat and mass transfer pipe or heat and mass transfer pipes. 2. The distillation unit according to claim 1, characterized in that the evaporator is made in the form of a heat exchanger consisting of a body and pipes, one of the chambers of which is connected to the (inner tube or ring) space of the distillation tower or column, while the other chamber is connected to the means for heating a mixed fluid (initial, separable mixture). 3. The distillation unit according to claim 1 or 2, characterized in that the means for heating the mixed fluid is a firebox, and the evaporator shirt is connected to the firebox. 4. Distillation unit according to one of paragraphs. 1-3, characterized in that the means for heating the coolant is a firebox and a jacket that is connected to the firebox. 5. The distillation unit according to one of claims 1 to 4, characterized in that the means for providing variable heat transfer is made in the form of a regulator of the level of fluid coolant in the annulus of the distillation column. 6. The distillation unit according to one of claims 1 to 5, characterized in that a pressure regulator is installed to supply the return of the coolant to the condenser. 7. A distillation plant according to one of claims 1 to 6, characterized in that the heat and mass transfer pipe or heat and mass transfer pipes have a variable wall thickness along their height. 8. A distillation plant according to one of claims 1 to 7, characterized in that the means for providing variable heat transfer is made in the form of plates or fins located on a heat and mass transfer pipe or heat and mass transfer pipes and having variable cross sections along the height heat and mass transfer tubes or heat and mass transfer tubes. 9. A distillation plant according to one of claims 1 to 8, characterized in that the means for providing variable heat transfer is made in the form of guide tubes mounted around the heat and mass transfer pipes at a certain radial distance and unevenly perforated along the height of the heat and mass transfer pipe or heat and mass transfer pipes. - 10 006452 10. A distillation plant according to one of claims 1 to 9, characterized in that the means for providing variable heat transfer are made in the form of guide tubes mounted around heat and mass transfer tubes at a certain radial distance and having variable internal cross sections along the height of the heat and mass transfer tubes or heat and mass transfer tubes, while the upper and lower parts of the guide tubes are interconnected with the annular space. 11. Distillation plant according to one of paragraphs. 1 -1 0, characterized in that the inner space of the heat and mass transfer tubes is partially or completely filled with heat transfer elements made in the form of spirals, the diameter of one of which is in a ratio of 1: 3 to 1: 5 with a smaller (inner) diameter of heat - and mass transfer tubes or heat and mass transfer tubes, while the ratio of the diameter of the spiral to the length of the spiral is from 1: 1 to 1: 3. 12. The distillation unit according to claim 5 or 6, characterized in that the fluid level regulator in the annular annular space of the column is made in the form of an external reservoir communicating by means of the coolant with the annular annular space of the distillation column. 1 3. Distillation plant according to one of paragraphs. 1 -1 2, characterized in that it is divided into vertical sections, while the inner tube spaces of the heat and mass transfer pipe or heat and mass transfer pipes between these sections are connected. 14. The distillation unit according to claim 13, characterized in that each section of the distillation column has its own annular annular space for a preferably different coolant. 15. The distillation unit according to item 13 or 14, characterized in that between the sections there are devices for sampling intermediate fractions. 16. The distillation plant according to Claim 15, wherein the inner cross-section of the heat and mass transfer tube or heat and mass transfer tubes in each subsequent section of the distillation column decreases in proportion to the flows of water vapor and / or phases of the fluid in the column. 17. A distillation plant according to one of claims 2-16, characterized in that the evaporator has horizontally mounted heating pipes, the cavities of the heating pipes being interconnected with the furnace chamber, and the annular annular space between the heating pipes and the body interconnected with the pipe space inside the heat and mass transfer tubes of the distillation column, as a result of which there is a free volume for the vapor phase at the top of the evaporator. 18. The distillation unit according to claim 17, characterized in that in the free volume at the top of the evaporator there are partitions with a perforated cross-section. 19. Distillation plant according to one of paragraphs. 1-18, characterized in that the evaporator is directly connected to the furnace chamber, and the distillation column is installed in the zone of the evaporator adjacent to the furnace chamber, while the end for the inlet of the initial mixture being separated is on the side of the evaporator opposite to the furnace chamber, and the end for the residue inlet is located in the lower zone of the evaporator adjacent to the furnace chamber. 20. A distillation plant according to one of claims 2-16, characterized in that the evaporator is made in the form of vertically directed heating pipes, the cavities of which are interconnected with the space (inner tube or annular space) of the heat and mass transfer pipe or heat and mass transfer distillation pipes columns, and the annular annular space between the heating pipes and the housing is interconnected with the furnace chamber. 21. The distillation unit according to claim 20, characterized in that the distillation column is mounted on the upper end of the evaporator, and the furnace chamber is connected, in the preferred embodiment, directly to the bottom of the annulus of the evaporator of the distribution ring collector. 22. The distillation installation according to item 21, characterized in that at the top of the annular annular space of the evaporator there is a second annular collector for flue gas discharge. 23. A distillation plant according to one of claims 20 to 22, characterized in that the evaporator has an inlet assembly for the initial separable mixture, which is located above the upper tube sheet of the evaporator, and an outlet unit for the residue is located under the lower tube sheet, whereby the evaporator has a jacket the cavity of which is connected to the chamber of the furnace. 24. A distillation plant according to one of claims 21 to 23, characterized in that the distribution ring collector or the second ring collector has or both have upper or lower partitions, respectively, for example, with annular gaps around the heating pipe or heating pipes. 25. The distillation apparatus according to paragraph 24, wherein the surfaces of the heating pipe or heating pipes located between the lower tube sheet and the lower partition are surrounded by protective sleeves with annular gaps around the heating pipes. 26. The distillation installation according A.25, characterized in that the gaps between the protective sleeve - 11 006452 mi and heating pipes are filled with insulating material. 27. The distillation unit according to claim 25, wherein the gaps between the protective sleeves and the heating pipes are filled with a fluidizing substance with a melting point not exceeding the decomposition temperature of the initial mixture and the decomposition temperature of the residue. 28. A distillation plant according to one of claims 20 to 27, characterized in that the surfaces of the heating pipes between the lower and upper partitions are surrounded by coaxially arranged restriction pipes. 29. Distillation unit according to one of paragraphs. 1-28, characterized in that the shirt means for heating the coolant is located at the bottom of the column. 30. Distillation unit according to one of paragraphs. 1-29, characterized in that the shirt means heating the coolant contains a reservoir in which the coolant is placed, and the upper level of this reservoir is below the column. 31. Distillation unit according to one of paragraphs. 1-30, characterized in that the coolant for the distillation section of the column is a liquid or mixed fluid with a boiling point in the range from the boiling point of the initial separable mixture to the boiling point of the lower boiling component of the distillate. 32. A distillation plant according to one of claims 1 to 31, characterized in that the carrier for the evaporating or evaporating section of the column is a liquid or mixed fluid with a boiling point in the range from the boiling point of the initial separable mixture to the boiling point of the higher boiling component of the residue. 33. The evaporation column having heat and mass transfer pipes according to one of claims 20-32, characterized in that the evaporation column has means for providing a variable degree of heat transfer along the height of the heat and mass transfer pipe or heat and mass transfer pipes between the spaces from the inside and outside of the pipe wall or pipe walls. 34. A distillation method for separating mixed fluids using a distillation unit according to one of claims 1 to 33, characterized in that it involves changing the degree of heat transfer along the height of the heat and mass transfer pipe or heat and mass transfer pipes between the spaces inside and outside of the wall pipes or pipe walls.