Installation for purification of the liquid hydrocarbon raw from methanol (versions)

FIELD: chemical industry; petrochemical industry; gaseous industry; oil-producing industry; oil-processing industry; installation for purification of the hydrocarbon raw from methanol.

SUBSTANCE: the invention is pertaining to the technology of purification of the hydrocarbon raw from methanol and may be used in gaseous, petroleum, petrochemical and chemical industries. The installation includes the assembly of the preliminary separation of the raw connected with the block of the adsorbing purification, the pipeline links and the shut-off-adjusting fittings. The assembly of the preliminary separation includes: the block of the preheating of the raw consisting of the heat exchangers (1) and (2), the rectifying column (3) with the connecting pipes for feeding of the liquid hydrocarbon raw (4), withdrawal of the methanol with the light fraction of hydrocarbons (5) and the withdrawal of the hydrocarbon tailings (6) with the bottom heating, the cooler (10) and container(11). The block of the raw preheating is connected to the connecting pipe (4) of the raw feeding into the rectifying column (3), and the connecting pipe (5) for the raw withdrawal in series through the raw preheating block, the cooler (10) and the container (11) directly connected with the block of adsorbing purification. In the other version the block of the raw preheating is connected to the connecting pipe (4) of feeding of the liquid hydrocarbon raw into the rectifying column (3), and the connecting pipe (5) of withdrawal through the heat exchanger (1) and the cooler (10) is connected to the connecting pipe (23) of the inlet into the extraction column. The connecting pipe (25) of withdrawal of the methanol with the light fraction of hydrocarbons out of the extraction column (20) is connected to the inlet connection pipe (28) of the separator (21), and the connecting pipe (26) of withdrawal of the water-methanol mixture is connected with the intermediate container (22). The connecting pipe (29) of withdrawal of the methanol with the light hydrocarbons from the separator (21) is connected to the block of the adsorbing purification. The connecting pipe (29) of withdrawal of the water-methanol mixture of the separator (21) is connected to the intermediate vessel (22), which outlet is connected to the feeding line of the extracting liquid into the extraction column (20). The invention reduces the operational costs, increases the lifetime of zeolite.

EFFECT: the invention ensures reduction of the operational costs, the increased lifetime of zeolite.

2 cl, 2 dwg, 2 ex

 

The invention relates to the technique and technology of purification of liquid hydrocarbons from methanol and can be used in gas, oil, refining, petrochemical and chemical industries.

The known method of gas purification from methanol carried out on the plant collection and preparation of gas in the messoyakha gas field (see "food preparation and processing of natural gas in the Messoyakha and South Soleninskoye fields - Scientific and technical review series: "Processing of gas and gas condensate", M, 1976, p.32-3 8), including a preliminary separation of gas from the liquid droplet adsorption and purging gas from water vapor and methanol.

A common feature of known and proposed methods is the adsorption of methanol.

The disadvantages of this method are incomplete extraction of methanol (only 20-25% of the original quantity), the impossibility of providing deep cleaning, because regeneration is a part of the crude gas containing methanol, heavy hydrocarbons and water, as well as a shorter lifetime of the zeolite due to its coking heavy hydrocarbons.

The closest in technical essence and the achieved result to the proposed technical solution is a method, implemented at the treatment plant sireny the hydrocarbon gases from methanol (see RF patent № 2120587, IPC6F 25 J 3/00, B 01 D 53/26, publ. in the official Gazette No. 29 from 20.10.98 year), including clean water, liquefied natural gas, separation of a mixture of liquefied petroleum gas and photometering mixture, the exhaust photometering mixture adsorption and purification of liquefied gas from methanol.

A common feature of known and proposed methods is the adsorption of methanol.

The disadvantage of this method of cleaning is the narrow range of raw materials used, as this method can be processed only light hydrocarbons, such as: propane, propane-butane fraction, LPG, liquefied petroleum gas, as in the processing of raw materials containing heavy hydrocarbons, the necessity of frequent replacement of the zeolite due to its coking heavy hydrocarbons, which, in turn, leads to unnecessarily high operating costs.

The technical problem of the invention consists in expanding the range of raw materials used, reducing operating costs, increasing service life of the zeolite at optimal operation of the adsorption treatment by quantitative and qualitative changes of the raw material supplied to the adsorptive purification.

This object is achieved in that in the method of purification of liquid hydrocarbons from methanol,comprising the adsorptive purification, pre hydrocarbons are divided into light and heavy fractions of parameters that ensure complete removal of methanol from the light fraction of hydrocarbons, which is subjected to an adsorption treatment, and the remaining fraction of heavy hydrocarbons divert.

In addition, the separated methanol with a light fraction of hydrocarbons is directed to contacting extracting the liquid, while distilling the methanol before it is calculated residual amount optimally adsorption purification.

In addition, the extraction of methanol from a mixture of light hydrocarbons carried out as a multistage process.

The proposed set of features allows this method to process not only easy hydrocarbon raw material, but raw material containing heavy hydrocarbon fractions, as the preliminary separation of the methanol from the light fraction of hydrocarbons from the heavy fraction of hydrocarbons in the technological parameters that ensure complete removal of methanol (i.e., when mode parameters of boiling methanol), allows for adsorption purification submit purposefully only methanol with a light fraction of hydrocarbons. Thus by removal of the fraction of heavy hydrocarbons after separation from methanol and light fraction of hydrocarbons increases the lifetime of the zeolite, on which they will not be coking heavy hydrocarbons, that allows to reduce operating costs.

The contacting of methanol and light fraction of hydrocarbons with extracting fluid, which can be multi-stage, allows for a higher content of methanol in liquid hydrocarbons (above 500 ppm) to remove the calculated amount of methanol, thereby ensuring optimal adsorption purification.

Known installation of collection and preparation of gas in the messoyakha gas field (see "food preparation and processing of natural gas in the Messoyakha and South Soleninskoye fields - Scientific and technical review series: "Processing of gas and gas condensate", M, 1976, p.32-38), containing the separator - filter for separating gas from the liquid droplet and the block adsorption purification, comprising adsorbers, with two adsorbers is in the process of adsorption of water vapor and methanol contained in the gas in the third - desorption process, the fourth process cooling. For desorption is used raw gas, part of which after separators comes in a tube furnace, and then in the adsorber regeneration of the adsorbent. The products of regeneration (water vapor and methanol), passing through a cyclone separator flow to the heat exchangers for cooling, and then into the separator, which separates liquid from gas. Gas from the top of the CE is arator is supplied to the adsorption, and separated in separators aqueous solutions of methanol arrive in the tanks.

Common features of known and proposed facilities are: block adsorption purification, piping and valves.

The disadvantages of the known installation is incomplete extraction of methanol from the gas phase (only 20-25% of the original quantity), the impossibility of providing deep cleaning, because regeneration is a part of the crude gas containing methanol, heavy hydrocarbons and water, a shorter lifetime of the zeolite due to its coking heavy hydrocarbons.

Closest to the technical essence and the achieved result to the present invention is a device for purification of liquefied hydrocarbon gases from methanol (see RF patent № 2120587, IPC6F 25 J 3/00, B 01 D 53/26, publ. in the official Gazette No. 29 from 20.10.98, containing site water rinse liquid hydrocarbons from methanol, which includes a device for extraction with nozzles of raw materials and water, coupled with the separator, provided with outlet nozzle photometering mixture, liquefied hydrocarbon gases, and the intermediate tank, the inlet nozzle which is connected to the supply line of make-up water, and the outlet nozzle via a pump connected to the pipe supplying water to the device for extraction, block also blonay cleaning, piping and valves and fittings.

Common features of known and proposed facilities are: block adsorption purification, piping and valves.

A disadvantage of the known installation is a narrow range of raw materials used, as this setting can be processed only raw materials containing light hydrocarbons, such as propane, LPG, NGL, and in the processing of raw materials containing heavy hydrocarbons, the necessity of frequent replacement of the zeolite due to its coking heavy hydrocarbons, which, in turn, leads to unnecessarily high operating costs.

The technical challenge is to expand the range of raw materials used, the increase in the lifetime of the zeolite, the reduction in capital and operating costs due to unloading of the adsorption columns on the quantity and quality of supply of raw materials.

This object is achieved in that the device for purification of liquid hydrocarbons from methanol, comprising an adsorption unit cleaning, piping and shut-off and control valves, it is further provided with a pre-separation of methanol from the light fraction of hydrocarbons from the heavy fraction of hydrocarbons that is connected to the adsorption unit PTS is tough.

In addition, the pre-separation unit includes heating of the substrate, a distillation column with a nozzle inlet and outlet and a heated bottom, refrigerator, capacity, and the output unit of the heating of the substrate is connected to the inlet nozzle in the distillation column, the top nozzle which successively through a heating unit of raw materials, a refrigerator and a capacity connected to the adsorption unit cleanup.

In addition, the pre-separation unit includes heating of the substrate, a distillation column with a nozzle inlet and outlet and a heated bottom, refrigerator, extraction column with a nozzle inlet and outlet, the separator and the intermediate tank, and the output unit of the heating of the substrate is connected to the inlet nozzle in the distillation column, the top nozzle through which the heating unit of raw materials and the refrigerator is connected to the inlet nozzle in the extraction column, the upper inlet of the extraction column is connected to the separator, and the lower intermediate capacity, in addition, the separator is connected to the adsorption unit cleaning, and also with an intermediate capacity, output of which is connected to the inlet nozzle extracting liquid in the extraction column.

The proposed set of features allows the separation of methanol from the light fraction of hydrocarbons from the heavy fraction Ugledar the Dov process at the facility is not only light hydrocarbons: propane, the propane-butane fraction, NGL, but also raw materials containing heavy hydrocarbon fractions, for example a hydrocarbon condensate, i.e. allows to extend the range of raw materials used. Excretion of installation of heavy hydrocarbon fractions after separation from methanol and light hydrocarbon fractions allows to unload the unit adsorption purification according to the quantity of supplied raw materials and deliver on adsorption purification of the total number of methanol, light hydrocarbons, which allows to optimize the adsorption treatment with the increase of the lifetime of the zeolite, as there is no coking zeolite heavy hydrocarbons, resulting in lower capital and operating costs.

Supply installation site pre-separation, including the heating unit of raw materials, distillation column, refrigerator and capacity, allows you to select the methanol with a light fraction in the gaseous state, to cool, condense and thereby to obtain a product, not containing heavy hydrocarbons, which is directed to an adsorption purification from methanol, and the heavy fraction that does not contain methanol, direct to the consumer.

Supply installation site pre-separation, including the heating unit of raw materials, distillation column, refrigerator, extraction column, the section of the tel and the intermediate tank, allows for a higher content of methanol in liquid hydrocarbons (above 500 ppm) to remove the calculated amount of methanol, thereby ensuring optimal performance of the unit adsorption purification.

The drawings show a schematic diagram of installation of purification of liquid hydrocarbons from methanol to implement the proposed method, in which figure 1 presents a scheme for processing of liquid hydrocarbons according to claim 1 of the formula of the invention, and figure 2 - claim 2.

The proposed method is carried out in the following sequence. A liquid hydrocarbon feedstock containing methanol (figure 1), heated and served in the distillation column 3, in which the raw material is pre-divided into light and heavy fraction of hydrocarbons in the technological parameters that ensure complete removal of methanol from the light fraction of hydrocarbons, i.e. regime parameters of boiling methanol. Methanol with a light fraction of hydrocarbons is cooled in the refrigerator 10 and fed into the container 11, and then on the adsorption treatment in one of the adsorbers 13, 14 block adsorption purification. Part of the heavy fraction of the hydrocarbon fuel in the furnace 9 and return to the bottom of the distillation column 3, and the remaining part is cooled in the regenerative heat exchanger 2 and divert.

With the increased is the obsession of methanol (figure 2) liquid hydrocarbons (above 500 ppm) pre-separated in a distillation column 3 methanol with a light fraction of hydrocarbons is cooled in the refrigerator 10 and fed into the extraction column 20 for engagement with the extracting liquid, such as water, while distilling the methanol before it is calculated residual amount optimally adsorption purification. Methanol with a light fraction of hydrocarbons after contact with the extracting fluid, which may be multi-stage, is sent to the separator 21, in which the main flow is separated photometadata mixture, and then a light fraction with a residual methanol content served on the adsorption treatment in one of the adsorbers 13, 14 block adsorption purification.

The treated light fraction of hydrocarbons after adsorption purification passes through the filter 15, which is captured gone with the flow of the raw material zeolite dust, and leaves the installation.

Example 1

Hydrocarbon condensate in the number 180000 kg/h at a temperature of 30°With the following fractional composition:

NC10%20%30%40%50%60%70%80%90%QC
28°49°64°79°91°105°119°138°177° 231°278°

and containing about 120 ppm of methanol and chlorides of alkali and alkaline earth metals through recuperative heat exchangers 1 and 2 is sent to distillation column 3, where the separation of raw materials into fractions of light and heavy hydrocarbons. Technological parameters of the column (P=0.15 MPa, Ttop=96°S, Tbottom=108° (C) are selected so that the methanol is completely transferred to the top product of the column is a light fraction of hydrocarbons of the following composition, wt.%: butane - 0,2; ISO-pentane to 18.7; n-petan - 3,8; hexane - 59,2; heptane - 8,9; octane - 7,6; nonan + above - 1,6. The concentration of methanol increases to 650 ppm. The bottom product of the column, representing the heavy fraction of the following composition, wt.%: ISO-pentane to 0.3; n-petan - 0,2; hexane - 32,0; heptane - 14,2; octane - 29,5; nonan - 7,3; Dean + above - 16.5, and flows into the intermediate tank 7 from which the pump 8 of the flow in the amount of 146800 kg/h is cooled in the regenerative heat exchanger 2 and is fed into the stream of treated light fraction of hydrocarbons coming out of the filter 15 after adsorbers 13, 14, and the remaining portion of the heavy fraction stream is heated in the furnace 9 and fed into the bottom of the distillation column 3. The top product of the distillation column 3, represents the methanol with the light fraction of hydrocarbons in the number 33220 kg/h, practiceguidelines the heat exchanger 1, the refrigerator 10 and enters the tank 11, from which the pump 12 is fed from the bottom up on adsorption purification from methanol for 24 h in one of the adsorbers 13, 14, filled with synthetic zeolite CAA. In the layer of adsorbent light hydrocarbons are purified to a residual content of 10 ppm methanol. The treated light fraction hydrocarbons passes through the filter 15, which is captured gone with the flow of the raw material zeolite dust and leaves from the plant. After the end of the cycle of the adsorption of light hydrocarbons removed a small amount of gas which is fed to the adsorber from the top down. The regeneration gas in the amount of 1400 nm3/h is heated in a furnace 19 to a temperature of 320-350°and served in the adsorber from the top down within 12 hours after the regeneration of the adsorber is translated to the stage of cooling. Cooling is carried out until a temperature of the gas at the outlet of the adsorber equal to 40-45°C. as regeneration gas and cooling use dry stripped gas.

Due to the fact that adsorption purification of subject light fraction of hydrocarbons, the process coking zeolite is significantly reduced, which leads to an increase of the lifetime of the zeolite with 1 to 3 years

Example 2

Hydrocarbon condensate in the number 180000 kg/h at a temperature of 30°With the following fractional composition:

PC10%20%30%40%50%60%70%80%90%QC
28°49°64°79°91°105°119°138°177°231°278°

and containing about 600 ppm of methanol and chlorides of alkali and alkaline earth metals through recuperative heat exchangers 1 and 2 is sent to distillation column 3, where the separation of raw materials into fractions of light and heavy hydrocarbons. Technological parameters of the column (P=0.15 MPa, Ttop=97°S, Tbottom=112° (C) are selected so that the methanol is completely transferred to the top product of the column is a light fraction of hydrocarbons of the following composition, wt.%: butane - 0,2; ISO-pentane to 18.7; n-petan - 3,8; hexane - 59,2; heptane - 8,9; octane - 7,6; nonan + above - 1,6. The concentration of methanol increases up to 2550 ppm, which leads to a significant increase in loading of the sorbent in the apparatus and thus to increase their overall mass. The bottom product of the column, representing the heavy fraction of the following composition, wt.%: ISO-pentane to 0.3; n-petan - 0,2; hexane - 32,0; heptane - 1,2; octane - 29,5; nonan - 7,3; Dean + above - 16,5 flows into the intermediate tank 7 from which the pump 8 of the flow in the amount of 137600 kg/h is cooled in the regenerative heat exchanger 2 and is fed into the stream of treated light fraction of hydrocarbons coming out of the filter 15 after adsorbers 13, 14, and another portion of the heavy fraction stream is heated in the furnace 9 and fed into the bottom of the distillation column 3. Methanol with a light fraction of hydrocarbons in the number 42400 kg/h passes recuperative heat exchanger 1, the refrigerator 10 and enters the extraction column 20 from the bottom up. Water in amount of 10 m3/h is fed by a pump 27 in the extraction column 20 from the top down to remove methanol to its residual content of 800 ppm optimally adsorption purification, and optionally clears the methanol with the light fraction of hydrocarbons from impurities.

When the limit concentration of 5 wt.% methanol in photometering mixture in the intermediate tank 22 of the extraction column 20 and the separator 21, a portion of this mixture is shown with installation, and the remaining part photometering mixture emerging from the intermediate tank 22, add fresh water in the amount of 1.3 m3/h and pump 27 back into the extraction column 20. From the top of the extraction column 20 methanol with light using hydrocarbon fraction is, saturated water flow to the separator 21 with shelf elements to effectively separated from the methanol and the light fraction of hydrocarbons water. Methanol with a light fraction of hydrocarbons from separator 21 by pump 12 serves on the adsorption cleanup within 24 hours in one of the adsorbers 13, 14, filled with synthetic zeolite CAA. In the layer of adsorbent light hydrocarbons are purified to a residual water content of 8 ppm and 10 ppm methanol. The treated light fraction hydrocarbons passes through the filter 15, which is captured gone with the flow of the raw material zeolite dust, and leaves the installation. After the end of the cycle of the adsorption of light hydrocarbons removed a small amount of gas which is fed to the adsorber from the top down. The regeneration gas in the amount of 1200 nm3/h is heated in a furnace 19 to a temperature of 320-350°and served in the adsorber from the top down within 12 hours after the regeneration of the adsorber is translated to the stage of cooling. Cooling is carried out until a temperature of the gas at the outlet of the adsorber equal to 40-45°C. as regeneration gas and cooling use dry stripped gas.

Due to the fact that adsorption purification of subject light fraction of hydrocarbons, the process coking zeolite is significantly reduced, which leads to an increase of the lifetime of the zeolite with 1 to 3 years.

Set the and purification of liquid hydrocarbons from methanol, presented in figure 1, contains the node pre-separation, which includes a heating unit of raw material, consisting of a regenerative heat exchangers 1 and 2; distillation column 3 from the nozzle 4 of the inlet of the liquid hydrocarbon, the pipe 5 release of methanol from the light fraction of hydrocarbons and socket 6 output fractions of heavy hydrocarbons, connected to the tank 7, the output of which by means of the pump 8 is connected through a heater 9 to distillation column 3 through recuperative heat exchanger 2 with the output line of the purified fraction of light hydrocarbons; refrigerator 10 and the container 11. Block heating of the substrate connected to the pipe 4 inputs in the distillation column 3. The nozzle 5 of the distillation column 3 is connected through the heat exchanger 1, the refrigerator 10, the container 11 and the pump 12 with the block adsorption purification.

The container 11 is a buffer tank in which collects methanol with a light fraction of hydrocarbons. From the raw material tank 11 with a certain flow enters the pump intake 12 in the tank 11 must always be a certain stock of raw materials. I.e. the container 11 is required for normal operation of the pump 12, as the supply of methanol with the light fraction of hydrocarbons directly from the pipeline complicates the operation of this pump.

Installation of purification of liquid hydrocarbons from methanol, before the purposes of figure 2, it contains pre-separation, which includes a heating unit of raw material, consisting of a regenerative heat exchangers 1 and 2; distillation column 3 from the nozzle 4 of the inlet of the liquid hydrocarbon, the pipe 5 release of methanol from the light fraction of hydrocarbons and socket 6 output fractions of heavy hydrocarbons, connected to the tank 7, the output of which by means of the pump 8 is connected through a heater 9 to distillation column 3 through recuperative heat exchanger 2 with the output line of the purified fraction of light hydrocarbons; refrigerator 10; extraction column 20, the separator 21 and the intermediate tank 22. Block heating of the substrate connected to the pipe 4 inputs in the distillation column 3. The nozzle 5 of the distillation column 3 is connected through the heat exchanger 1 and the refrigerator 10 with the socket 23 of the extraction column 20. The extraction column 20 also has an outlet 24 of the filing of the extracting fluid, such as water pipe 25 yield of methanol with the light fraction of hydrocarbons after contact with the extracting fluid and the pipe 26 output photometering mixture, which is connected to the intermediate tank 22. The outlet 25 of the extraction column 20 is connected to the inlet side 28 of the separator 21. The separator 21 has a socket 29 output photometering mixture connected with the intermediate tank 22, and Petrovac output of methanol, light hydrocarbons, connected through the pump 12 with the block adsorption purification. The output from the intermediate tank 22 is connected to the supply line extracting fluid through the pump 27 with the outlet 24 of the extraction column 20.

Block adsorption purification consists of adsorbers 13, 14, the output of which is connected to the filter device 15 and is also the site of regeneration gas consisting of filter 16, refrigerator 17, the separator 18 and the furnace 19.

Installation of purification of liquid hydrocarbons from methanol works as follows. A liquid hydrocarbon feedstock containing methanol passes through recuperative heat exchangers 1, 2 and enters the distillation column 3, where the separation of raw materials for light and heavy fractions. Technological parameters of the column chosen so that the methanol is completely transferred to the top product of the column representing a light fraction of hydrocarbons, i.e. modal parameters boiling methanol. The bottom product of the column, representing the heavy fraction of hydrocarbons, enters the intermediate tank 7 from which part of the flow passing through the furnace 9 is returned into the distillation column 3, and the other part stream is cooled in the regenerative heat exchanger 2 and is fed into the stream of treated light fraction of hydrocarbons coming out of the filter 15 after the adsorption treatment. Ver is the average product of the distillation column 3, representing the methanol with the light fraction of hydrocarbons through the recuperative heat exchanger 1 and the refrigerator 10 enters the tank 11, from which the pump 12 is fed from the bottom up in one of the adsorbers 13, 14, filled with synthetic zeolite, adsorption purification from methanol.

With increased content of methanol in the liquid hydrocarbons (above 500 ppm) methanol with a light fraction of hydrocarbons after the refrigerator 10 is directed to the extraction column 20, in which the pump 27 is fed downwards extracting the liquid, for example water, to extract the methanol to its residual content optimally adsorption purification. In addition, the water cleanses the methanol with the light fraction of hydrocarbons and impurities.

From the top of the extraction column 20 light fraction of hydrocarbons from a residual methanol content and saturated water enters the separator 21 with shelf elements to effectively separate drip photometering mixture, which is then discharged into the intermediate tank 22.

The bottom product of the extraction column 20, which represents photometering mixture, also fed into the intermediate tank 22 from which the pump 27 is returned to the extraction column 20.

When the limit on the concentration of methanol in odometer the th mixture, coming in the intermediate tank 22, a portion of this mixture is shown with installation, and the remaining part photometering mixture emerging from the intermediate tank 22, add fresh water and pump 27 back into the extraction column 20 on the circulation, which improves the extraction process.

From separator 21 methanol with a light fraction of hydrocarbons dissolved until the equilibrium state water comes from the bottom up on adsorption purification from methanol and water in one of the adsorbers 13, 14, filled with synthetic zeolite.

Purified in one of the adsorbers 13, 14 light fraction hydrocarbons passes through the filter 15, which is captured gone with the flow of the raw material zeolite dust and leaves from the plant. After the end of the cycle of the adsorption of light hydrocarbons removed a small amount of gas which is fed to the adsorber from the top down. The regeneration gas is heated in the furnace 19 to a temperature of 320-350°and served in one of the adsorbers 13, 14 from the top down. Upon completion of the regeneration of the adsorber is translated to the stage of cooling. Cooling is carried out until a temperature of the gas at the outlet of the adsorber equal to 40-45°C. as regeneration gas and cooling use dry stripped gas.

1. Installation of purification of liquid hydrocarbons from methanol, including pre times the population of raw materials, connected to the adsorption unit cleaning, piping and shut-off and control valves, wherein the node is pre-separation unit includes heating of the substrate, distillation column with connections to the inlet of the liquid hydrocarbon feedstock, the yield of methanol with the light fraction of hydrocarbons and exit of heavy hydrocarbon fractions and heated bottom, refrigerator, capacity, and the output unit of the heating of the substrate is connected to the inlet nozzle of the liquid hydrocarbon in a distillation column, and the outlet nozzle of methanol with the light fraction of hydrocarbons successively through a heating unit of raw materials, a refrigerator and a capacity connected to the adsorption unit cleanup.

2. Installation of purification of liquid hydrocarbons from methanol, including pre-separation of the material containing device for extraction, the intermediate tank, the separator and connected to the adsorption unit cleaning, piping and shut-off and control valves, wherein the node is pre-separation of the raw material is further provided with a heating unit of raw materials, distillation column with connections to the inlet of the liquid hydrocarbon feedstock, the yield of methanol with the light fraction of hydrocarbons, the output of heavy hydrocarbon fractions and heated bottom, fridge, while the output of the block is and the heating of the substrate is connected to the inlet nozzle of the liquid hydrocarbon distillation column, the outlet nozzle of methanol with the light fraction of hydrocarbons distillation column through a heating unit of raw materials and the refrigerator is connected to the inlet nozzle in the extraction column, the outlet nozzle of methanol with the light fraction of hydrocarbons extraction columns is connected to the inlet side of the separator and the outlet nozzle photometering mixture of the extraction column with an intermediate tank, and the outlet nozzle of methanol light hydrocarbon specified separator is connected to the adsorption unit clean, and the outlet nozzle photometering mixture separator is connected with an intermediate capacity, the output of which is connected to the supply line extracting liquid in the extraction column.



 

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11 cl, 3 dwg, 2 tbl

FIELD: gas treatment.

SUBSTANCE: invention relates to novel catalysts, which can be, in particular, used in automobile engine exhaust treatment, in processes of deep oxidation of toxic organic impurities in industrial emission gases, and in other applications. Adsorption-catalytic system, including granules of sorbent capable of sorbing at least one of reagents and catalyst, represents geometrically structured system wherein catalyst is made in the form of microfibers 5-20 μm in diameter, sorbent granules are disposed inside catalyst, and size ratio of sorbent granules to catalyst microfibers is at least 10:1. Catalyst microfibers are structured in the form of woven, knitted, or pressed material. Gas treatment process involving use of such system is based on that gaseous reaction mixture to be treated is passed through above-defined system while periodically varying temperature of mixture, in particular raising it, to accomplish or regeneration of sorbent.

EFFECT: enhanced process simplicity and reliability (simple process government system, absence of mechanical stream switching devices, reduced power consumption, and enabled continuous gas treatment.

2 cl, 2 ex

FIELD: heat technology.

SUBSTANCE: invention relates to technology for treatment of smoke gases from sulfur dioxide. Method for treatment of smoke gases from sulfur dioxide involves passing smoke gases through countercurrent scrubber with absorption liquid based on ammonia aqueous solution for preparing ammonium sulfite followed by oxidation of ammonium sulfite to ammonium sulfate. Then one part of absorption solution removing after oxidation is mixed with fresh ammonium aqueous solution and fed to treatment of smoke gases and another part is fed to utilization. Oxidation is carried out with smoke gases oxygen in indicated scrubber in addition initiating agent for oxidation to absorption liquid as azocompounds. Invention provides simplifying the process and to reduce time for accumulation of ammonium sulfite by 1.8-2.0-fold.

EFFECT: improved method for treatment.

FIELD: production of aluminum in cells with self-fired anodes, possibly processes for cleaning anode gases.

SUBSTANCE: method comprises steps of accumulating anode gases, preliminarily combusting them together with air in burner devices mounted in cells; supplying gas-air mixture after preliminary combustion of anode gases along gas duct to stage of dust and gas trapping and blowing out to atmosphere. Before supplying gas-air mixture from burner devices to stage of dust and gas trapping, it is fed to process for oxidizing roasting; heated up to temperature 800-1100°C and then it is cooled until 230-290°C and heat is used for production needs.

EFFECT: lowered content of carbon, resin and CO in exhaust gases.

Arunachaleswarar // 2241526
The invention relates to the field of purification of atmospheric air directly to the device neutralize the harmful components of the gas emissions aeropastale settlements

The invention relates to an improved absorbent composition comprising an aqueous solution of piperazine and methyldiethanolamine intended for removal from gas streams acidic gases such as CO2H2S and COS

FIELD: production of aluminum in cells with self-fired anodes, possibly processes for cleaning anode gases.

SUBSTANCE: method comprises steps of accumulating anode gases, preliminarily combusting them together with air in burner devices mounted in cells; supplying gas-air mixture after preliminary combustion of anode gases along gas duct to stage of dust and gas trapping and blowing out to atmosphere. Before supplying gas-air mixture from burner devices to stage of dust and gas trapping, it is fed to process for oxidizing roasting; heated up to temperature 800-1100°C and then it is cooled until 230-290°C and heat is used for production needs.

EFFECT: lowered content of carbon, resin and CO in exhaust gases.

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