The method of processing of gas condensate

 

(57) Abstract:

Usage: petrochemistry. Essence: from the condensate separated from the gas. Unstable gas condensate is subjected to contacting with a zeolite-containing catalyst at 250 - 430oC, a pressure of 0.1 to 1.5 MPa. Produce is subjected to rectification to give the fuel fractions. Use preferably the catalyst composition, % wt: zeolite Y with a molar ratio of SiO2/Al2O3from 4.0 to 8.0 - 0,05 - 5,0, high-silica zeolite with a molar ratio of SiO2/Al2O3from 20,0 to 100.0 - 0,05 - 85,0, matrix - rest. The finishing is carried out at flow rate of feed of 0.5 - 3.5 m3/m3including the Rectification is carried out in the presence of gaseous products of the process of refining and/or gas rectification. 3 C.p. f-crystals, 2 tab., 1 Il.

The invention relates to the refining and petrochemical industries, namely the processing of gas condensate from the production of motor fuels and fuel formed by mixing the individual fractions isolated from the condensate.

Known methods of processing hydrocarbon material extracted from wells include two stages. The first stage of processing on promyslovosti installations. The second stage processing of the prepared raw material for refineries, including primary and secondary processing (I. A. Gurevich "Technology of oil and gas processing", h I, M. Chemistry, 1972, S. 153 198).

Secondary processing of hydrocarbons in the fuel are such basic processes as the processes of reforming of straight-run gasoline, naphtha fractions, the cracking of oil fractions, wikipaedia more than 200oC (Cm. A. I. Vladimirov "catalytic reforming", M. 1993, s 8 26). There are various schemes of the organization of secondary processes (reforming) using a variety of hydrocarbons and catalytic systems.

For example, there is a method of improving the quality naphtha fractions, including fractionation of the feedstock naphtha light fraction and heavy fraction. The heavy fraction is subjected to reforming to aromatics and octane number.

Part of the flow of the reformer is mixed with the light fraction and subjected to reforming over zeolite catalyst ZS M-5. Receive a stream of hydrocarbon enriched in aromatics, which can be divided into fractions. (Patent Velicer. N 2034351, C 10 F 59/00, 1980).

The known is SUP>oC by multi-stage catalytic reforming followed by distillation of the obtained liquid products, and the rectification of liquid products of reforming are emitting head of the faction wikipeida from the initial boiling point of up to 130 - 160oC and the residual, wikipeida from 130 160oC until the end of the boil and then mix in a certain ratio. (Ed. mon. N 1766945, C 10 G 35/04, 16.10.1989).

In the known methods of producing high octane gasoline, performed at the factory, as a source of raw materials used hydrocarbon fraction, the receipt of which from gas-and-oil raw materials involves many technological operations, which complicates the process as a whole.

Closest to the proposed method to the technical essence and the achieved result is a method of processing gas in motor fuel, separating gas from condensate multistage separation in the oil fields and the subsequent processing of the raw gas condensate and volatile factory settings. Processing of unstable condensate includes:

remove from condensation of the methane-ethane fraction (separation at a temperature of 30oC);4(NGL);

destructive processing of condensate, including preliminary deep Hydrotreating stabilization section of hydrogenated feed and subsequent fractionation (distillation) with the release of factions since the beginning of the boil 62oC 62 85oC, 85 180oC. Fraction 62 85oC and 85 - 180oC is subjected to catalytic improvement in equipment of the type L-35-II/1000, followed by distillation and producing high-octane gasoline. The reforming process is carried out at a temperature of 450 530oC, a pressure of 1.5 to 3.0 MPa, and space velocities of 1.2 to 1.5 h-1("Technology of processing of sulfurous gas and condensate" edited Vakulin Century. And. Orenburg, 1990, S. 103 129).

The disadvantage of the prototype is a complex technology of processing of gas condensate in motor fuel, due to the commercial preparation of the condensate for transport to the factory and complex processing factory, including the stage of stabilization, fractionation, Hydrotreating of the obtained fractions, catalytic refining and distillation. In addition, as a rule, released by condensate stabilization and fractionation of light hydrocarbons is fed to the processing and lost (burned), which reduces the yield of the target topsite provides the possibility of processing in the area of gas condensate production, with the production of motor fuels, while a simplification of the process, and increase output of high-quality fuel fractions due to involvement in the processing of additional quantities of light hydrocarbons and regulate the output of gasoline, kerosene and diesel fractions.

The problem is solved by the proposed method for processing of gas condensate, including the separation of gas from liquid phase and recycling of unstable condensate in motor fuels using catalytic refining and distillation, the distinctive feature of which is that beautification is subjected directly to the unstable condensate in the presence of a zeolite catalyst at a temperature of 250 430oC, a pressure of 0.1 to 1.5 MPa, after which the produce is subjected to rectification with the selection of the target fuel fractions.

Preferably the process of gentrification should be conducted using a zeolite-containing catalyst having the following composition, wt. zeolite Y with a molar ratio of SiO2/Al2O3equal to from 4.0 to 8.0, 0,05 5,0, servicecompany zeolite with a molar ratio of SiO2/Al2O3equal to from 20 to 100, 0,05 85,0, matrix - OYA 0.5 to 3.5 m3/m3h), and the process of rectification in the presence of gaseous products formed during catalytic sweetening and/or gas rectification.

The combination of these features allows to significantly simplify the technology of processing of gas condensate and implement it directly on the fields; to increase the output of motor fuels by engaging in the process of processing the fraction of light hydrocarbons dissolved in the unstable condensate and get these products with high consumer properties (see data table 2); to regulate the ratio of the outputs of petrol, diesel and kerosene fractions, by regulating the temperature conditions of the process and composition of the used catalyst.

The drawing shows a schematic diagram of an installation for the production of motor fuels by the proposed technology.

The installation includes a separator 1 for separating gas from the condensate, the finishing reactor 2, the rectifying column 3.

The method is as follows: the gas from the well into the separator 1 (or system separators, high and low pressure), where the separation of raw gas from condense light hydrocarbon into the reactor 2, where at a temperature of 250

430oC, a pressure of 0.1 to 1.5 MPa, the space velocity of the raw material of 0.5 to 3.5 m3/(m3h) in the presence of the zeolite catalyst is in the process of gentrification.

As the zeolite catalyst can be used any known catalysts containing zeolites sverkhvysokochastotnye type pentasil or zeolite type Y, which introduced various inorganic binder clay, alyumooksid, silica, metroselect and so on (see for example, A. S. N 1594768, B 01 J 29/08, 1983 A. S. N 1594767, B 01 J 29/08, 1983 A. S. N 1396334, B 01 J 29/12, 1982, A. S. N 1396333, B 01 J 29/12, 1984 Pat. G B N 2034351, C 10 G 59/00, 1980; EP N 0032414, C 10 G 59/02, 1981; JP N 54-23362, C 10 G 37/10, 1979, and so on).

The best results were obtained on the catalyst comprising a mixture of the two zeolites zeolite of type Y with a molar ratio of SiO2/Al2O3equal to 4,0oC8,0, in the amount of 0.05 to 5.0 wt.%. and sverkhvysokochastotnogo zeolite with a molar ratio of SiO2/Al2O3equal to 20 to 100, in the amount of 0,05 85,0, matrix else.

Zeolite Y and servicecompany zeolite included in the catalyst composition may be used in rare-earth ion-exchange form, and/or H-shape, and/or Zn-forms. The/SUB>, amorphous aluminosilicates, zirconosilicate, etc. In the process of finishing the formation of the catalyzate isoparaffin and aromatic hydrocarbons, which contribute to higher octane and cetane numbers of motor fuels. The resulting produce (liquid reaction products) are then fed into the distillation column 3, where the selection of the following oils: gasoline N. K. 120oC 120 140oC or 120 160oC, or 120 180oC or 120 - 200oC, or N. K. 200oC and kerosene-diesel fraction 200 - 350oC. the Process of rectification, it is advisable to conduct in the presence of gaseous products formed during catalytic sweetening and/or gas rectification, which perform the role of inert gases. Then depending on seasonal needs fuels get summer and winter varieties of automotive and diesel fuels by mixing gasoline and diesel fractions in a certain ratio.

Characteristics used unstable condensates obtained from the Department of gascondensate raw gas are presented in table 1.

The following examples illustrate the method, but not ohranyayuschie it.

Zeolite Y and servicecompany zeolite in the Na-forms are mixed with a matrix, is formed in the form of extrudates, pellets, pastilles and then carry out ion exchange of cations Na+on rare and/or cations of Zn+2and/or H+, washed with water, dried and calcined (examples 3, 8, 13 to 16).

Example 1. An aqueous solution of aluminum sulfate concentrations of 20 kg/m3on Al2O3and containing 80 kg/m3H2SO4, an aqueous solution of sodium silicate concentration of 130 kg/m3on SiO2and containing 65 kg/m3NaOH, aqueous suspension of zeolite NaY and sverkhvysokochastotnogo zeolite concentration, respectively, 1.4 and 140,0 kg/m3mixed at the temperature of 15oC C the formation of hydrogel with a pH of 8.5. Then the hydrogel was processed with an aqueous solution of ammonium sulfate concentration of 10 kg/m3when temperature 50oC for 24 hours, washed with distilled water at 50oC for 24 hours, dried at 170oC and calcined at 550oC in air for 12 hours. Get a catalyst of the following composition: zeolite Y in N vokalnym ratio of SiO2/Al2O3100 5% rest of the matrix is amorphous aluminosilicate.

Example 2. Catalytic improvement of unstable condensate is carried out at 250oC and space velocity of the feedstock 0.75 m3/(m3h) and a pressure of 1.5 MPa by using a catalyst having the composition, wt. zeolite Y in rare form with a molar ratio of SiO2/Al2O3equal 5,2 5,0% zeolite servicecompany in the protonated form with a molar ratio equal to 40 25% rest of the matrix pseudoboehmite.

Example 3. Catalytic improvement of unstable condensate is carried out at 430oC, space velocity of the raw materials 3.5 m3/(m3h) and a pressure of 0.1 MPa by using a catalyst having the composition, wt. zeolite Y in the H form with a molar ratio of SiO2/Al2O3equal to 8.0, 0.05% zeolite servicecompany in the protonated form with a molar ratio of SiO2/Al2O3100, 5% rest of the matrix is amorphous aluminosilicate.

Example 4. Catalytic improvement of unstable condensate is carried out at 275oC, space velocity of the raw material 2.5 m3/(m3h) and a pressure of 0.5 MPa using a catalyst having the composition, vysokokremnievykh in Zn-shaped with a molar ratio of SiO2/Al2O3equal to 20, 50% rest of the matrix - g-Al2O3.

Example 5. Catalytic improvement of unstable condensate is carried out at 350oC, space velocity of the raw material 1.5 m3/(m3h) and a pressure of 0.2 MPa using a catalyst having the composition, wt. zeolite Y in Zn-shaped with a molar ratio of SiO2/Al2O3; equal to 4.8, 1,0% servicecompany zeolite in the H form with a molar ratio of SiO2O3equal to 60, 0.5% of the rest of the matrix is amorphous zirconosilicate.

Example 6. Catalytic improvement of unstable condensate is carried out at 400oC, space velocity of the raw material 2.0 m3/(m3h) and a pressure of 0.1 MPa by using a catalyst having the composition, wt. zeolite Y in the H form with a molar ratio of SiO2/Al2O3equal to 5.1, 1.5% zeolite servicecompany in rare form with a molar ratio of SiO2/Al2O360, 30% of the rest of the matrix - a-Al2O3.

Example 7. Catalytic improvement of unstable condensate is carried out at 300oC, flow rate of feed of 1.0 m3(m3h) and a pressure of 1.0 MPa when using the catalysate is th 7,2, 5.0% zeolite servicecompany in Zn-shaped with a molar ratio of SiO2/Al2O3100, 0.05% of the rest of the matrix is amorphous magnicient.

Example 8. Catalytic beautification gas condensate is carried out at 375oC, space velocity of the raw material 1.5 m3/(m3h) and a pressure of 0.1 MPa by using a catalyst having the composition, wt. zeolite Y in the H form with a molar ratio of SiO2/Al2O3equal to 4.8, 1.0% zeolite servicecompany in the protonated form with a molar ratio of SiO2/Al2O3equal to 45, 85% of the rest of the matrix boehmite.

Example 9. Catalytic improvement of unstable condensate is carried out at 250oC, flow rate of feed of 1.0 m3/(m3h) and a pressure of 0.1 MPa by using a catalyst having the composition, wt. the zeolite in the H-and rare forms with a molar ratio of SiO2/Al2O3equal to 5.1, 3.5% of the zeolite servicecompany in the protonated form with a molar ratio of SiO2O3equal to 65, 20% rest of the matrix g-Al2O3.

Example 10. The catalyst as in example 9. Catalytic improvement of unstable condensate is carried out at 350oC, flow rate is political colouration of unstable condensate is carried out at 430oC, flow rate of feed of 1.0 m3/(m3h) and a pressure of 0.1 MPa.

Example 12. The catalyst as in example 9. Catalytic improvement of unstable condensate osushestvliayut at 375oC, flow rate of 1.5 m3/(m3h) and a pressure of 0.5 MPa.

Example 13. Catalytic improvement of unstable condensate is carried out at 400oC, space velocity of the raw material 1.5 m3/(m3h) and a pressure of 0.25 MPa by using a catalyst having the composition, wt. zeolite Y in the N - and rare forms with a molar ratio of SiO2/Al2O3equal to 70, 1.5% of the rest of the matrix is amorphous zirconosilicate.

Example 14. The catalyst as in example 13. Catalytic improvement of unstable condensate is carried out at 400oC, flow rate of feed of 1.0 m3/(m3h) and a pressure of 0.1 MPa.

Example 15. The catalyst as in example 13. Catalytic improvement of unstable condensate is carried out at 375oC, flow rate of feed of 1.0 m3/(m3h) and a pressure of 1.5 MPa.

Example 16. Catalytic improvement of unstable condensate is carried out at 430oC, flow rate under the t Y in the N - and rare forms with a molar ratio of SiO2/Al2O3equal to 5.1, 25% rest of the matrix is amorphous zirconosilicate.

Example 17. Catalytic improvement of unstable condensate is carried out at 375oC, space velocity of the raw material 1.5 m3/(m3h) and a pressure of 0.2 MPa using a catalyst having the composition, wt. zeolite servicecompany in N - and rare forms with a molar ratio of SiO2/Al2O3equal to 70, 5.0% of the rest of the matrix is amorphous magnicient.

The obtained samples catalyzate in the process of elevating unstable condensate (examples 2 to 17) is subjected to distillation in the presence of gaseous products formed during the processing of unstable condensate and/or rectification. Temperature catalyzate at the entrance of the distillation column is 270 320oC and a pressure of 0.12 to 0.20 MPa.

The results of the experiments are presented in table 2.

Thus the advantage of the proposed method is:

possibility of production wells in the area of operation, which will give an opportunity to save costs for the preparation of well production to transportation, transportation and delivery of motor fuels in place is piracy (respectively AIDS);

the increase in the output of motor fuels at the expense of involvement in the processing of light hydrocarbons;

obtaining high-octane gasoline with an octane rating of up to 85 98 and diesel fuels with pentanoyl number 45 54 with the output up to 93.7% wt

the ability to adjust the output of gasoline and diesel fractions depending on the needs in a particular type of fuel.

1. The method of processing of gas condensate, including the separation of gas from liquid phase, processing the received unstable condensate in motor fuels using catalytic refining and distillation, characterized in that the improvement is subjected directly to the unstable condensate in the presence of the zeolite catalyst at 250 430oC, 0.1 to 1.5 MPa, after which the produce is subjected to rectification with the selection of the target fuel fractions.

2. The method according to p. 1, characterized in that the finishing is carried out in the presence of a zeolite-containing catalyst composition, wt.

The zeolite of type V with a molar ratio of SiO2/Al2O34 8 - 0,05 5,0

High-silica zeolite with a molar ratio of SiO2/Al2O320 100 0,05 85,0

Matrix Else

3. Spas 3.5 m3/m3h

4. The method according to p. 1, characterized in that the rectification catalyzate carried out in the presence of gaseous products formed during the catalytic refining, and/or gas rectification.

 

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FIELD: chemistry.

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FIELD: chemistry.

SUBSTANCE: invention refers to production method of high-octane gasoline fractions and/or aromatic hydrocarbons C6-C10 as follows, hydrocarbon materials is heated, evaporated and overheated to process temperature, thereafter providing its contact at temperature 320-480°C and excess pressure with periodically recyclable catalyst containing zeolite of composition ZSM-5 or ZSM-11. Then it is cooled. Contact products are partially condensed, separated into gaseous and liquid fractions by separation. Liquid products of separation are supplied as power primarily to the first distillation column for separation of hydrocarbon gases and liquid stable fraction. The latter is supplied to the second distillation column for separation of high-octane gasoline fraction, or aromatic hydrocarbon fraction, and heavy charge fraction. Gaseous fraction resulted from separation of contact products is supplied to the first distillation column, specifically to intermediate section between infeed and external reflux inlet. External reflux is liquid distillate of the first distillation column.

EFFECT: reduction of power inputs, i.e. quantities of heat and cooling agent, required for reaction products separation.

5 cl, 2 ex

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