Method of hydrocarbons processing (versions)

FIELD: petroleum refining industry; methods of separation of hydrocarbons at stabilization of petrol or conversion products of synthesis gas.

SUBSTANCE: the invention is pertaining to the field of petroleum refining industry, in particular, to the methods of separation of hydrocarbons at stabilization of gasoline or the synthesis gas processing products. The method of processing of hydrocarbons according to the first version includes feeding of the liquid hydrocarbons into the rectifying column, withdrawal from its lower part of the residue and from its upper part - of a steam-gaseous phase, which is cooled in the refrigerator-condenser and partially condensed. The produced gas-liquid mixture is separated for a condensate and a steam-gaseous phase. Then a part of the condensate taken in the capacity of a reflux is fed into the rectifying column, and the other part of the condensate taken as a distillate is withdrawn according its destination. At that the steam stripped steam-gaseous phase is fed into the recuperative heat exchanger and after condensation of a part of a steam-gaseous phase separate the produced condensation moisture. The separated gas phase is fed into a vortex pipe for its separation into a cold stream and a hot stream. At that the cold stream is directed into the recuperative heat exchanger as a cooling medium. The cold stream heated in the recuperative heat exchanger and the hot stream both are withdrawn in compliance with their destination and the condensate from the separator is mixed with the withdrawn distillate. According to the second version the method provides for feeding of the synthesis gas into the synthesis column and withdrawal from it of a gases mixture containing a synthesis product and the unreacted synthesis gas. The gases mixture is directed into the refrigerator-condenser, in which the synthesis product is condensed and then the mixture is separated for a condensate and a steam-gaseous phase. The condensate is withdrawn in compliance with its destination. One part of the steam-gaseous phase is used as a blowdown gas, and the other part is returned into the synthesis column for reprocessing. At that the blowdown gas is directed into the recuperative heat exchanger, in which a part of the blowdown gas is condensed. Then the condensate is separated from the gas phase. The produced gas phase is fed into the vortex pipe, where the gas phase is separated for a cold stream and a hot stream. The cold stream is fed into the recuperative heat-exchanger as a medium for cooling the blowdown gas. The cold stream heated in the heat exchanger and the hot stream both are withdrawn as required. The blowdown gas condensate is withdrawn from the separator and fed to the consumer. The technical effect is increased efficiency of the hydrocarbons processing, decreased losses of products at their separation.

EFFECT: the invention ensures increased efficiency of the hydrocarbons processing, decreased losses of products at their separation.

4 cl, 2 dwg

 

The invention relates to the field of oil refining, mainly to methods for processing hydrocarbons, in particular to a method of stabilizing gasoline in distillation columns and methods of synthesis of hydrocarbons, methanol and other organic compounds.

A method of refining hydrocarbons, including the supply of raw materials in the distillation column and the removal from it of the residue, the side straps and vapor phase (see SU 910725, CL 10 G 7/06, 07.03.82).

However, this method of refining petroleum and its products requires a lot of energy and complex technological scheme for its implementation, which reduces the attractiveness of this method of processing.

The closest to one of the variants of the invention the technical essence and the achieved result is a method for processing of liquid hydrocarbons, including the supply of liquid hydrocarbon in a distillation column, the removal of the bottom residue and with top - vapor phase, the latter after exiting the column is cooled in the cooler-condenser and partially condensed, after which the gas-liquid mixture is separated into condensate and depleted vapor vapor-gas phase, then part of the condensate as phlegmy served in the distillation column, and the other part of the condensate as distillate output imposed on the structure (see Plonowski A.N., Nikolaev P.I., the Processes and apparatuses of chemical and petrochemical technology, Moscow, Chemistry, 1987, s-283).

The closest to another variant hydrocarbon processing is a method for processing hydrocarbons comprising feeding the synthesis gas to the synthesis column and the removal from it of a mixture of gases containing product synthesis and unreacted synthesis gas, a mixture of gases is directed to the cooler-condenser, which condenses the product of synthesis, then divide the mixture on the condensation product of synthesis and gas-vapor phase, and then the condensate output by appointment, part of the vapor phase output as the purge gas, and the other part of the return in the synthesis of re-processing (see Overmantel, Equipment synthesis of high pressure in the nitrogen industry Chemistry, Moscow, 1970, p.61-62).

However, one of the main disadvantages of these methods of processing hydrocarbon is the loss of part of the product hydrocarbon processing, and at the same time a sufficiently high pressure vapor phase at the output of the rectifying column and the purge gas in place its output in units of synthesis useless choked, resulting in a loss of pressure, as a form of energy.

Task to be solved by the present invention is directed, is to increase the efficiency of how re is abode hydrocarbons by reducing food loss processing due to the useful life of the pressure of the vapor phase and the purge gas after the release of their respective distillation columns and columns synthesis and, as a consequence, an increase in the yield of distillate and product synthesis.

This task is solved by a method for processing hydrocarbons in the first embodiment includes a supply of liquid hydrocarbon in a distillation column, the removal of the bottom residue and with top - vapor phase, the latter after exiting the column is cooled in the cooler-condenser and partially condensed, after which the gas-liquid mixture is separated into condensate and depleted vapor vapor-gas phase, then part of the condensate as phlegmy served in the distillation column, and the other part of the condensate as distillate output destination, with depleted vapor vapor-gas phase is sent to the regenerative heat exchanger in which by cooling condense a portion of the depleted steam vapor phase, and then separating the obtained regenerative heat exchanger condensate from the gas phase, after which the gas phase is directed to a vortex tube split at the last gas phase on the cold and hot streams, while the cold stream is directed to the recuperative heat exchanger as environment, cooling depleted steam combined-cycle phase, and then heated in a recuperator cold flow and hot flow output destination, and the condensate from the separator is mixed with the output of distillate.

Depleted steam combined cycle phase before entering the regenerative heat exchanger can be pre-cooled in an additional refrigerator.

The specified task according to the second variant is solved by a method for processing hydrocarbons involves feeding the synthesis gas to the synthesis column and the removal from it of a mixture of gases containing product synthesis and unreacted synthesis gas, a mixture of gases is directed to the cooler-condenser, which condenses the product of synthesis, then divide the mixture on the condensation product of synthesis and gas-vapor phase, and then the condensate output by appointment, part of the vapor phase output as the purge gas, and the other part of the return in the synthesis of re-processing, while the purge gas is sent to the regenerative heat exchanger, where by cooling condense a portion of the purge gas, and then separate the produced regenerative heat exchanger condensate purge gas from the gas phase, after which the gas phase is directed to a vortex tube split at the last gas phase on the cold and hot streams, while the cold stream is directed to the recuperative heat exchanger as environment, cooling the purge gas, and then heated in a recuperator cold flow and hot flow output destination,and the condensate purge gas from the separator output to the consumer.

The purge gas before it enters the regenerative heat exchanger can be pre-cooled in an additional refrigerator.

In the course of the research it was found that one of the major drawbacks of the methods of processing hydrocarbon is a partial loss-products (distillate and product synthesis)contained in depleted gas-vapor phase and in the purge gas. Used refrigerators do not allow to fully achieve condensation of vapor distillate and product synthesis, which leads to the loss of gas "sduwqhu" valuable hydrocarbons, such as gasoline fractions or products of synthesis. The pressure in the zone of the outlet vapor phase from the top of the distillation column may reach 0.5 MPa To 0.8 MPa, and the pressure in the output location of the purge gas can reach tens of MPa. This relatively high pressure vapor phase and the purge gas allows you to organize more effective condensation product processing (distillate and product synthesis) after its release from the distillation column and synthesis column.

As shown by the analysis, the proposed method allows to increase the amount of condensate distillate and product synthesis from the vapor phase and the purge gas through the efficient use of energyadvice, accordingly depleted steam vapor phase and the purge gas, which reduces the loss of distillate and product synthesis. This was achieved through the use of energy pressure depleted steam vapor phase and the purge gas for cooling. As a consequence, deeper cooling depleted steam vapor phase and the purge gas allows to intensify the process of condensation, respectively distillate and product synthesis depleted steam vapor phase purge gas and to improve the environmental safety of the processes of hydrocarbon processing. As a result, the combustion is fed gas-vapor phase, which has only relatively light hydrocarbons, which reduces the harmful products of combustion in the flue gases, and in the case of the synthesis process in the purge gas dramatically increases the amount of inert, environmentally safe gas.

Thus, were able to achieve these in the invention objectives - improving the efficiency of processing of hydrocarbons by reducing losses of distillate and product synthesis through the use of pressure depleted steam vapor phase and the purge gas after the release of the latest from the distillation column and synthesis column. Simultaneously Powys who stayed environmental safety of the process of hydrocarbon processing.

Figure 1 shows the schematic diagram of the setup that implements the described method for processing of liquid hydrocarbons by distillation, and figure 2 presents a schematic diagram of the setup processing of synthesis gas.

Setting processing of hydrocarbons by distillation (see figure 1) contains the distillation column 1 is connected to it by a pipe 2 for supplying liquid hydrocarbons, pipe 3 exhaust residue and a pipe 4 exhaust vapor phase. The latter is connected through a cooler-condenser 5 to the separator-column 6, which is the exit of the condensate is connected to the top of the distillation column 1 and line 7 removal of distillate, and the output of depleted steam vapor phase to the recuperative heat exchanger 8, which, in turn, is connected to the separator 9. The separator 9 condensate output is connected to the pipe 7 removal of distillate, and the output of the gas phase to the vortex tube 10 connected thereto by pipes 11 and 12 respectively drainage hot and cold streams. While the pipeline 11 outlet cold stream is connected to a regenerative heat exchanger 8. The unit can be equipped with an additional refrigerator 13, installed in front of the recuperative heat exchanger 8.

Installation for processing of hydrocarbons, in particular the synthesis gas, with the holding synthesis 14 connected to the pipe 15 of the feed synthesis gas and pipeline 16 exhaust gas mixture, which is connected through a cooler-condenser 17 to separator 18 synthesis gas. The separator 18 synthesis gas yield of the condensation product of synthesis is connected to the pipe 19 discharge of product synthesis and the release of vapor phase to the synthesis column 14 by typing in her synthesis gas, for example, by means of pipe 27. In addition, the output of the vapor phase from separator 18 synthesis gas is connected to the pipe 20 to the outlet purge gas, which, in turn, through the recuperative heat exchanger 21 is connected to the separator 22 purge gas. The separator 22 exit condensate purge gas is connected to the pipe 19 discharge of product synthesis and the release of the gas phase to the vortex tube 23 with the pipes 24 and 25 respectively drainage hot and cold streams of gas phase. The pipeline 24 withdrawal cold flow of the gas phase is connected to the recuperative heat exchanger 21. The unit can be equipped with an additional refrigerator 26, installed in front of the recuperative heat exchanger 21.

The described method for processing hydrocarbons, such as distillation, liquid hydrocarbons, is implemented as follows. Liquid hydrocarbons are heated and served on the pipeline 2 in the distillation column 1. From the bottom of the distillation column via line 3 assign the remainder, and in line 4 divert steam gas the first phase. Last after exiting the column 1 is cooled in the cooler-condenser 5 and partially condense. The resulting gas-liquid mixture in the separator 6 is separated into condensate and depleted steam combined-cycle phase. Then part of the condensate as phlegmy served in the distillation column 1, and another part of the condensate as a distillate through the pipeline 7 is removed from the installation processing of hydrocarbons on purpose, such as storage tanks for distillate. Depleted vapor vapor-gas phase from the separator 6 is directed to the recuperative heat exchanger 8, in which by cooling condense a portion of the depleted steam vapor phase. Then in the separator 9 separates the obtained regenerative heat exchanger 8, the condensate from the gas phase, after which the gas phase is directed to a vortex tube 10 with the division in the last of the gas phase on the cold and hot streams. Cold flow through the pipeline 11 is sent to the regenerative heat exchanger 8 as the environment, cooling depleted steam combined-cycle phase. Heated in a recuperator 8 cold flow and hot flow through the pipeline 12 output destination, for example as fuel in the furnace of the boiler unit. The condensate from separator 9, which is a condensation of the distillate is sent to the pipeline 7 technical disti late and mixed with the output of distillate. The processes in the regenerative heat exchanger 8 and the separator 9 may be implemented in a single device, for example in a modernized regenerative heat exchanger 8. In this heat exchanger 8 through the cooling will occur not only condensation process part of the depleted steam vapor phase, and separating the condensate from the gas phase. Depleted steam combined cycle phase before entering the regenerative heat exchanger 8 can be pre-cooled in an additional refrigerator 13. This cooling procedure may be necessary when working in hot conditions, for example in the summer.

In the case of the second variant of the method of processing hydrocarbon synthesis 14 serves on the pipeline 15 synthesis gas and divert it through the pipeline 16 a mixture of gases containing product synthesis and unreacted synthesis gas. The mixture of gases is directed to the cooler-condenser 17, which condense product synthesis. After that, the separator 18 is divided mixture of the condensation product of synthesis and gas-vapor phase. This condensate by pipeline 19 is removed from the installation by appointment, for example in the reservoir for storage product synthesis. Part of the vapor phase from separator 18 output as the purge gas through the pipeline 20 and the other part is returned to the synthesis column 14, for example, the R, the pipe 27 for reprocessing. The purge gas through the pipeline 20 is directed to the recuperative heat exchanger 21, where by cooling condense a portion of the purge gas. Then in the separator 22 separates the obtained regenerative heat exchanger 21 condensate purge gas from the gas phase, after which the gas phase is directed to a vortex tube 23 with the division in the last of the gas phase on the cold and hot streams. Cold flow through the pipeline 24 is directed to the recuperative heat exchanger 21 as the environment, cooling the purge gas, and then heated in a recuperator 21 cold flow and hot flow through the pipeline 25 output destination, such as combustion in the boiler plant and the condensate purge gas (product synthesis synthesis column 14) from the separator 22 output destination, for example in line 19. The processes in the recuperative heat exchanger 21 and the separator 22 may be implemented in a single device, for example in a modernized recuperative heat exchanger 21. In this recuperative heat exchanger 21 through the cooling will occur not only condensation process part of the purge gas, and the separation formed by condensation from the gas phase. The purge gas before entering the recuperator is a heat exchanger 21 can be pre-cooled in an additional refrigerator 26. This cooling procedure may be necessary when working in hot conditions, for example in the summer.

The present invention can be used in chemical, oil and gas industry for distillation of petroleum and petroleum products, as well as in the synthesis of ammonia, methanol and other chemical products.

1. Method for processing hydrocarbons comprising a supply of liquid hydrocarbon in a distillation column, the removal of the bottom residue and with top - vapor phase, the latter after exiting the column is cooled in the cooler-condenser and partially condensed, after which the gas-liquid mixture is separated into condensate and depleted vapor vapor-gas phase, then part of the condensate as phlegmy served in the distillation column, and the other part of the condensate as distillate output destination, wherein the depleted steam vapor-gas phase is sent to the regenerative heat exchanger in which by cooling condense a portion of the depleted steam vapor phase and then separate the produced regenerative heat exchanger condensate from the gas phase, after which the gas phase is directed to a vortex tube split at the last gas phase on the cold and hot streams, while the cold stream is directed to regenerating the exchanger as the cooling medium depleted vapor vapor-gas phase, then heated in a recuperator cold flow and hot flow output destination, and the condensate from the separator is mixed with the output of distillate.

2. The method according to claim 1, characterized in that the depleted steam vapor-gas phase before entering the regenerative heat exchanger is pre-cooled in an extra refrigerator.

3. Method for processing hydrocarbons comprising feeding the synthesis gas to the synthesis column and the removal from it of a mixture of gases containing product synthesis and unreacted synthesis gas, a mixture of gases is directed to the cooler-condenser, which condenses the product of synthesis, then divide the mixture on the condensation product of synthesis and gas-vapor phase, and then the condensate output by appointment, part of the vapor phase output as the purge gas, and the other part of the return in the synthesis of re-processing, wherein the purge gas is sent to the regenerative heat exchanger in which by cooling condense a portion of the purge gas and then separate the produced regenerative heat exchanger condensate purge gas from the gas phase, after which the gas phase is directed to a vortex tube split at the last gas phase on the cold and hot streams, while the cold stream is sent to the regenerative heat exchanger in ka is este environment, cooling purge gas, and then heated in a recuperator cold flow and hot flow output destination, and the condensate purge gas output to the consumer.

4. The method according to claim 3, characterized in that the purge gas before it enters the regenerative heat exchanger is pre-cooled in an extra refrigerator.



 

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