Pentane isomerization process

FIELD: petrochemical processes.

SUBSTANCE: pentane-into-isopentane isomerization is carried out on platinum catalyst (IP-62) at 370-395°С, pressure 2.302.7 MPa, and hydrogen-to-hydrocarbon molar ratio (0.2-0.8):1, preferably 0.5:1.

EFFECT: enhanced process efficiency and reduced power consumption.

3 dwg, 3 ex

 

The invention relates to the production of products of isomerization, in particular of isopentane pentane, and can be widely used in the synthetic rubber industry, in the production of the basic monomer is isoprene. Isopentane is a raw material in the process of dehydrogenation of isopentane to isoprene, as a component of high-octane gasoline as a solvent, etc.

A known method of obtaining of isopentane pentane catalyst FE-62 with the output of the target product is not less than a 49.5 wt.% on missing raw materials at temperatures up to 430°and the pressure in the system to 4.0 MPa [1]. Closest to the invention to the technical essence is a method of producing isopentane isomerization of normal pentane, which consists in passing the prepared and heated feedstock through a bed of the catalyst FE-62 in the presence of hydrogen in a molar ratio of H2:na5H12=(2-3):1, at a temperature of 360-430°C. thus Obtained a mixture of products is cooled and separated into a gaseous hydrogen-containing mixture is sent again in the isomerization process and the isopentane - pentane fraction is directed to the separation by rectification [1].

As can be seen from the above, this process is a high temperature (up to 430°C), energy-intensive, with high pressure (up to 4.0 MPa), using the pain is th number of hydrogen what makes the process extremely vzryvoopasnym.

The purpose of this invention is the selection of such a process so that when doubled the load on raw (pentane)to reduce consumption of raw materials (hydrogen, pentane), and energy (fuel gas. electricity, prom. water), while reducing vzryvoopasnosti.

This goal is achieved on the same catalyst FE - 62 when the change process by reducing the molar ratio of hydrogen:pentane, reducing the pressure and temperature.

In the production of obtaining isopentane as a result of increasing load on raw more than twice [Project Giprokauchuk On accretion power in Sterlitamak JSC “caustic”] 14000 kg/h up to 30,000 kg/h, was not successful accretion performance compressors (POS), which is not possible to increase the mass rate of isomerization process with 1 to 1.5 h-1and the pressure in the system is scheduled to 4.0 MPa. And it is not possible to withstand the molar ratio of hydrogen - pentane (2-3):1, which decreased the yield of isopentane, which was brought to the norm (49,5%) by increasing the temperature from 380°With up to 405°With with increase energy. All this was forced to seek an alternative to the existing process.

In [2] shows the effect of partial giving the value of pentane to the reaction rate of isomerization, it shows the influence of the partial pressure of hydrogen in the depth of the isomerization of pentane and shows the influence of the molar ratio of hydrogen:pentane to a depth of isomerization.

Therefore, it is advisable to carry out the process of isomerization of pentane at a lower molar ratio hydrogen:pentane, valid from the point of view of the preservation stability of the catalyst; low ratio of gas circulation should also contribute to less entrainment of isopentane with the circulating gas in the reaction zone [2].

On the basis of the conducted research (experiments) was chosen as the new way, different from that used in industry, namely with the double load (with 14000 kg to 30,000 kg).

1. Changed the molar ratio of hydrogen:pentane (2-3):1 to (0,2-0,8) of 0.5:1, which resulted in lower consumption of hydrogen with 80 m3up to 30 m3and less than one ton of produced isopentane.

2. Reduced operating pressure in the system isomerization with a 3.5-4.0 MPa to 2.3-2.7 MPa.

3. Reduced the temperature in the reaction zone to 380°while increasing the yield of isopentane 1.0 to 3.5%, i.e. from 49.5% to 53% or more.

According to regulations, the isomerization process occurs on the platinum catalyst FE-62 in three stages. In the beginning there is the removal of hydrogen (dehydrogenation) on the metal part of the catalyst, then recombination (isomerization) on the basis of acid on the fluorine who happens again restore (hydrogenation). The presence of excess hydrogen shift reaction dehydrogenation in the field of hydrogenation.

EXAMPLE 1.

According to regulations, the isomerization process was conducted with the following parameters.

1. Raw materials (pentane), kg/h - 14 000

2. Circulating H2total (100%), m3/h - 13600(10880)

3. System pressure, MPa - 3,4-4,0

4. Temperature, ° - 360-430

5. The output of the iC5H12, wt.% not less than 49,5

6. Output(C1-C4), wt.% - 1,5-2,0

7. The consumption of H21 ton iC5m3- 80

8. The molar ratio of N2:na5- (2-3):1

EXAMPLE 2.

After increasing the load on raw (1985) more than 2 times the isomerization process was conducted with the following parameters.

1. Raw materials (pentane), kg/h - 30000

2. Circulating N2total (100%), m3/h - 13600(9520)

3. System pressure, MPa - 2,8-3,2

4. Temperature, ° - 375-420

5. The output of the iC5H12, wt.% not less than a 49.5-51

6. Output (C1-C4), wt.% - 1,4-1,8

7. The consumption of H21 ton iC5m3, - 50

8. The molar ratio of N2:na5, - (1-1,9):1

EXAMPLE 3. (proposed optimal)

By changing the molar ratio of N2:na5H12=(0,2-0,8) 0,5:1, got the following technological mode isomerization.

1. Raw materials (pentane), kg/h 30 000

2. Circulating H2total (100%), m3/h - 5837 (4670)

3. The pressure in the system is e, MPa - 2,3-2,7

4. Temperature, ° - 370-395

5. The output of the iC5H12, wt.% not less than a 50.5-53,0

6. Output (C1-C4), wt.% - 1,0-1,4

7. The consumption of H21 ton iC5m3- 30 or less

8. The molar ratio of H2: na5- (0,2-0,8)0,5:1

Thus it is seen that at lower molar ratio of the downward flow of hydrogen thereby reduced the energy potential of the system isomerization, and reducing the output side (C1-C4products with a higher yield of isopentane. The proposed method differs molar ratio of hydrogen:pentane, the pressure in the system isomerization, and the temperature in the reaction zone. The use of this technological mode allows the following :

1. By changing the molar ratio of hydrogen:pentane (2-3):1 to (0,2-0,8), preferably up to 0.5:1, to reduce the consumption of hydrogen for the production of 1 ton of isopentane more than 2 times, i.e. from 80 m3up to 30 m3or less.

2. To reduce the pressure in the system isomerization from 3.4-4.0 MPa to 2.3-2.7 MPa.

3. To reduce the temperature in the reaction zone is 10-20°while increasing the yield of isopentane from 49.5 wt.% to 50.5-53 wt.%, i.e. by 1.0-3.5 wt.%.

4. To reduce the molar content of hydrogen in the system isomerization 4-6 times that can reduce the explosion hazard of the process, i.e. to translate it into a zone of flammable range

5. To reduce the consumption of fuel gas by reducing the amount of circulating gas and by reducing the temperature in the isomerization zone.

6. To reduce the energy consumption, since one compressor can be submitted circulating gas at the same time on two of the isomerization unit.

See figures 1-3 show:

figure 1 - the effect of molar relationship of H2:na5at a depth of isomerization of normal pentane;

figure 2 - effect of temperature on the depth of the isomerization of pentane;

figure 3 - the effect of partial pressure of hydrogen in the depth of the isomerization of pentane.

Sources of information

1. Directory of refiners. L.: Chemistry, 1986, s-190 - prototype.

2. Nurburing. Technology isomerization of paraffin hydrocarbons. L.: Chemistry, 1985.

3. Cthomas. Industrial catalytic processes and effective catalysts. M.: Mir, 1973, p.28-32.

The way isomerization of pentane to isopentane on the platinum catalyst FE-62, characterized in that the isomerization is carried out at a temperature 370-395°C, the pressure of 2.3-to 2.7 MPa, a molar ratio of hydrogen:hydrocarbon equal to (0,2-0,8):1, preferably of 0.5:1.



 

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