Method for producing enriched c2h4the fraction of the hydrocarbon product from the original faction

 

(57) Abstract:

Obtaining enriched C2H4- fraction of the product includes the separation of purified and dried hydrocarbon original fraction by single or multi - stage partial condensation of the separate components. The fraction of this division, enriched WITH2H6, is subjected to cracking, and then the cracking gas, enriched in N2/S2H4/ C2H6brought to the same distillation method of division as hydrocarbon source faction, and after stirring it is separated into its components. The method has only one low-temperature part that allows to refuse from the relaxation of the turbines, which reduces investment and operating costs. 4 C.p. f-crystals, 1 Il.

The invention relates to a method for obtaining enriched C2H4- fraction of the product from the purified, in particular, is exempt from CO2and dried hydrocarbon original faction.

Methods of separation of hydrocarbon gas mixtures, in particular of natural gas, known for a long time. As follows from the well-known way of separating C2+- hydrocarbon fraction of gas after the first partial condensation is served in the distillation column, in which the separation of the methane fraction and C2+- hydrocarbon fraction. The values of temperature and pressure required for rectification, are achieved by heat transfer and two-stage powerful relaxation. Often this installation for the separation of natural gas connected additional unit for further processing C2+- hydrocarbon fraction. If it is, for example, installing ethylene, C2+- hydrocarbon fraction from the plant for the separation of natural gas passes first stage separation of C2/C3. Then C2the hydrocarbons are subjected to cracking and finally again by distillation of low-temperature separation of exempt from the first H2and CH4before being split C2H4/C2H6can be obtained from the product fraction C2H4. However, this method requires at least 2 low-temperature installation, as well as additional connected thereto stage separation. To provide the necessary cooling in these low-temperature installations in accordance with tiled application Germany N 3441307 required several relaxare cooling inside the ethylene units for low-temperature separation used a propane or propylene and ethylene convection cooling.

Closer analogue to the invention is a method for producing enriched C2H4-fraction of the product from the purified, in particular, is exempt from CO2and dried hydrocarbon source fractions, in particular natural gas, by its division into separate components using partial condensation and rectification (DE 2505689 B2, 21.04.77).

The present invention is the elimination of the deficiencies of the prior art, in particular the creation of a method of obtaining a C2H4-fraction of the product with lower investment and production costs.

This object is achieved by a method for producing enriched C2H4-fraction of the product from the purified, in particular, is exempt from CO2and dried hydrocarbon source fractions, in particular, natural gas by its division into separate components using partial condensation and rectification, in which, according to the invention, the purified and dried hydrocarbon source fraction separated by one - or multi-stage partial condensation of the separate components, the fraction enriched in C2H6this razdel separation as hydrocarbon source fraction by single or multi - stage partial condensation and after mixing with her share components, in particular, also enriched C2H4-product fraction.

In this preferred:

(a) purified and dried hydrocarbon source fraction is cooled and separated by one - or multi-stage partial condensation;

b) a fraction enriched in C1+with stage a) of the method together with the fraction enriched in H2/C2H4/C2H6with stage d) of the method is directed first to the degree of separation of C1/C2where by rectification removes C1-hydrocarbons and H2;

b) a fraction enriched in C2+from stage b) of the method is directed to the step of separation of C2/C3at which removes C3+- hydrocarbons;

g) a fraction enriched in C2from stage C) of the method is directed to the step of separation of C2H4/C2H6where get enriched C2H4-product fraction;

d) a fraction enriched in C2H6with stage d) of the method is directed to the cracking process;

(e) fraction enriched in H2/C2H4/C2H6with stage d) method after washing, hydrogenation and drying also subjected to single or multi - stage partial condensation and then p is 1+ with stage a) of the method.

Preferably the contents of C2H6in the hydrocarbon fraction is at least 10 mol.%, preferably 20 mol.%, in particular, 30 mol.%.

Further, preferably single or multi - stage partial condensation of the purified and dried hydrocarbon source fractions, and also pre-treated with the cracking gas enriched in H2/C2H4/C2H6exercise in General low-temperature device.

In addition, preferably formed at the stage C) method C3+- hydrocarbons by distillation is separated into a heavy hydrocarbon components and these components are at least partially directed to the cracking process.

The advantage offered by the invention of the method relative to known methods is that the General method has only one low-temperature part and attached thereto required under division (C1/C2, ACC. C2/C3and C2H4/C2H6. This means, firstly, that the required space is reduced to one plant working according to this method, and storagestation costs. In addition, reduced ongoing operating costs, as in the low temperature range, it is now possible to refuse from the relaxation of the turbines.

The invention, as well as other options for its implementation are explained in more detail using the drawing.

The drawing shows a schematic representation of the method according to the invention. Through line 1 to the compressor device A is supplied by natural gas, which is first compressed by the supply pressure from about 10 to about 30 bar. This compression is usually performed using a single-stage compressor. Then compressed natural gas is cooled by means of cooling air and is supplied to the device for separation of CO2. Removal of CO2of compressed natural gas can be achieved by different well-known specialist of ways. This applies, as a rule, chemical leaching. Using chemical cleaning of the content of CO2natural gas is reduced to about 50 parts per million. Then natural gas is fed through line 1 to a drying device C. In the drying device C natural gas first, again pre-cooled, and the temperature of the preliminary klaio offered adsorption unit pressure change, consisting of at least two adsorbers, one adsorber operates in the adsorption mode, while the second adsorber is regenerated. By use of an adsorbent by means of adsorption can be deleted a large part of the remaining natural gas CO2. Then cleaned and dried natural gas is fed through line 2 to a low-temperature device D. it natural gas is separated by one - or multi-stage partial condensation until then, until you skondensirovat all of ethane and heavy hydrocarbon fraction and a part of the methane fraction. To a low-temperature device D through the pipe 4 in addition is supplied also pre-processed and received at a specific stage pre-treatment of the cracking gas enriched in H2/C2H4/C2H6. The cracking gas is also single or multi - stage partial condensation until condenseries all of ethane and ethylene fraction. The gaseous fraction obtained in the individual stages of condensation forming in the enriched H2the gas fraction, the so-called fuel gas. All condensate fraction of natural gas, soo is 2 through the pipeline 12, 11 respectively. Step E division C1/C2consists mainly of the distillation column, which in the appropriate places summarizes the flow of the condensate formed inside the low-temperature device D. From the head of the distillation column through line 6 is shown a gaseous fraction consisting mainly of methane. This gaseous fraction forms a so-called gas. C2+- hydrocarbon fraction from the lower portion of the distillation column is fed through line 13 to the degree F of division C2/C3. Step F division C2/C3consists mainly of a distillation column, which is in contrast to the distillation column of stage E division C1/C2operating at approximately 26 bar, runs at about 24 bar. In the lower part of the column is formed C3+- hydrocarbon fraction, which is discharged through line 14. This C3+- hydrocarbon fraction can be separated into other stages of separation of C3- C4-, respectively, C5+- hydrocarbon fraction. Part of the obtained fraction C3covers mechanical losses of the circulating cooling C3. the ladenia for olefin production. C2- hydrocarbon fraction formed in the head of the distillation column of stage F division C2/C3slurry is fed through line 15 to the degree G of division C2H4/C2H6. Step G division C2H4/C2H6consists mainly of a distillation column operating at about 19 bar. In the head of this distillation column is formed fraction C2H4- product and is excreted through the pipeline 7. Formed in the lower part of the distillation column fraction C2H6is fed through line 3 to the device H for cracking and sudden cooling. Between devices G and H, as a rule, provides buffer solution C2H6that is, in the case of short-term reduce the amount of natural gas that prevents disabling device for cracking and sudden cooling. In addition, by using accumulated in it C2H6, faster resume start the installation. The main part of the device H for cracking and rapid cooling are pyrolysis furnace used for thermal cleavage (cracking) of hydrocarbon. Pyrolysis furnace for degradation of hydrocarbons is described, the Albanian from the device H for cracking and sudden cooling is supplied through the pipe 3' to the device K for the Department of water. In it the cracking gas is cooled to the dew point temperature of water, so that together with water from the cracking gas removes particles of coke, tar and heavy petroleum distillates. Before cleared the cracking gas is led through the pipe 3 into the device L hydrogenation, it undergoes a multi-stage, preferably a five-speed compression to about 37 bar. After each stage of compression before submitting to the next stage of compression of the cracking gas is cooled and the resulting condensates are removed. These condensates are composed mainly of water and heavy hydrocarbons. Hydrocarbons can also be fed to the above mentioned degrees of separation for C3+- hydrocarbon fractions. In the device L hydrogenation occurs catalytic hydrogenation of the cracking gas for the selective conversion contained in the cracking gas of acetylene to ethylene. The device L hydrogenation consists mainly of isothermal working tubular reactor. The catalyst is generally within the reactor tubes. Cooling of the reactor tubes by using evaporating the methanol, and the methanol after separation ridculously H2/C2H4/C2H6after pre-cooling (not shown) and adsorption drying (not shown) through line 4 goes, as already described, to a low-temperature device D. Propane or propylene and ethylene convection cooling, prepared to obtain fractions of C2H4product on the steps E, F or G division C1/C2C2/C3or C2H4/C2H6and in the low-temperature device D allows the method according to the invention to refuse used before relaxation turbines, as this convection cooling also provides sufficient cooling for the separation of natural gas.

1. Method for producing enriched C2H4- fraction of the product from the purified, in particular, is exempt from CO2and dried hydrocarbon source fractions, in particular, natural gas by its division into separate components using partial condensation and rectification, wherein the purified and dried hydrocarbon source fraction separated by one - or multi-stage partial condensation to separate componey H2/C2H4/C2H6directed to the division as the hydrocarbon source fraction by single or multi - stage partial condensation and after stirring it is divided into components, in particular, also enriched C2H4- product fraction.

2. The method according to p. 1, characterized in that a) the cleaned and dried hydrocarbon source fraction is cooled and separated by one - or multi-stage partial condensation; b) a fraction enriched in C1+ from stage a) of the method together with the fraction enriched in H2/C2H4/C2H6with stage d) of the method is directed first to the degree of separation of C1/C2where by rectification removes C1-hydrocarbons and H2C) a fraction enriched in C2+ from stage b) of the method is directed to the step of separation of C2/C3at which removes C3+-hydrocarbons; d) fraction enriched in C2from stage C) of the method is directed to the step of separation of C2H4/C2H6where get enriched C2H4the product fraction; d) fraction enriched in C2H6with stage d) of the method is directed to the cracking process; (e) francissca also subjected to single or multi - stage partial condensation and then before submitting to the degree of separation of C1/C2(stage b) of the method) is mixed with the fraction enriched in C1+with stage a) of the method.

3. The method according to p. 1 or 2, characterized in that the content of C2H6in the hydrocarbon fraction is at least 10 mol.%, preferably 20 mol.%, in particular 30 mol.%.

4. The method according to PP.1 to 3, characterized in that the single or multi - stage partial condensation of the purified and dried hydrocarbon source fractions, and also pre-treated with the cracking gas enriched in H2/C2H4/C2H6exercise in General low-temperature device.

5. The method according to PP.1 to 4, characterized in that formed on the stage) method C3+-hydrocarbons by distillation is separated into a heavy hydrocarbon components and these components are at least partially directed to the cracking process.

 

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