SU1567604A1 - Method of dewaxing distillation petroleum products - Google Patents

Abstract

The invention relates to petrochemistry, in particular to the dewaxing of distillate petroleum products to produce paraffins, which are raw materials for the chemical and microbiological industries. The purpose of the invention is to increase the yield of paraffins and improve its quality. Dewaxing of distillate petroleum products is carried out by treating them with a solution of urea in isopropyl alcohol, separating the complex formed from the deparaffinate, followed by a stepwise washing of the complex with an oil fraction, decomposing the complex to release paraffins. The final stage of the washing of the complex is carried out at a temperature corresponding to the crystallization temperature of the urea solution. The yield of the target paraffins 86.8 - 87.7%. 1 ill., 1 tab.

Description

The invention relates to the petrochemical industry, namely to the carbamide dewaxing of distillate petroleum products with the production of paraffins, which are valuable as raw materials for the chemical and microbiological industry, these paraffins must contain no more than 0.5% of aromatic hydrocarbons, and In the future, it is planned to reduce the content of aromatic hydrocarbons to 0.01%.

The purpose of the invention is to increase the yield of liquid paraffin and improve its quality and lower the freezing temperature of the dewaxed fuel.

The drawing shows the implementation of the method

In the reactor 1, the diesel distillate is mixed with a solution of urea in isopropyl alcohol of concentration 6P - 80% at a temperature of 35-60 ° C. within 60 min. After complexing, the reaction mixture (the complex and the deparaffinate) through line 2 enters the mixer 3, where it is mixed with the extract solution of the third stage of the washing of the complex. The diluted reaction mixture was fed through line 4 to a sump. 5 To separate the deparaffinate solution from the suspension of the complex. Dilution of the deparaffinate with the extract solution (fr. 100-140 ° C) reduces its viscosity and specific gravity, as a result of which sludge with

Further, the complex suspension according to line 6 is directed to a three-stage washing. The extraction solution in line 7 enters the mixer 8, where at the final dewaxing temperature the first stage of counterflow washing is carried out with a fraction of 150-200 ° C.

After the first washing stage, the complex with the extract solution along line 9 is sent to a sump 10 for separation. In the sump 10, the extract solution is separated and, via line 11, is sent for regeneration. After separation from the extract solution. the complex through line 12 is sent to the mixer 13 to the second stage of counter-flushing, where via line 14 the regenerated washing fraction from the first stage of washing is supplied. After the second stage of washing, the complex with the extract solution through line 15 enters the sump 6. The complex and the sump 16 through line 17 are directed to the third stage of the washing in mixer 18 where the line 19 is supplied with a washing fraction 100-140 ° C, unsaturated with isopropyl alcohol ,,

To obtain maximum purity paraffins, the washing is carried out at the crystallization temperature of the urea solution.

After the third stage of washing, the complex and the extract solution through line 20 are sent to a sump 21 ". After separation, the washed complex through line 22 is directed to decomposition (not shown in the diagram), and the extract solution through line 23 - to the reaction mixture after the complexation stage to a mixer 3

Deparated fuel with an extract solution and isopropyl alcohol from clarifier 5 through line 24 enters column 25 for regeneration. After regeneration, isopropyl cake through line 26 is returned to the reactor, which makes it possible to maintain a high concentration of isopropyl alcohol for maximum extraction of n-alkanes from raw materials to improve the waxy properties of the dewaxed product. The gasoline fraction 100-140 ° C via line 19 is directed to the third stage of flushing, and dewaxed fuel via line 27 is removed from the process.

According to the described scheme, the yield of target paraffins is 86.8 - 87.7% with a high degree of purity (not more than 0.01%) due to the involvement of paraffins boiling at a temperature of 180 - 265 ° C in the target fraction. In addition, the freezing point of the deparaffinag decreases from –30 ° C to –44 ° C.

The conditions of the method and the results are shown in the table.

one

For dewaxing, a diesel distillate of 180 - 350 ° C is taken, the content of complexing n-alkanes in which is 28.5 wt.%.

Concentration of isopropyl alcohol in solution, wt.% 70 Solution to raw materials ratio, w / w 4: 1 Complexation time, min 60

The amount of the washing fraction supplied to the washing of the massed complex to the feedstock the decomposition temperature of the complex and you

dividing paraffins, C 75

Claims (1)

Invention Formula The method of dewaxing distillate petroleum products by processing 67604b their solution of carbamide in isopropyl alcohol, separating the complex formed from the deparaffinate, followed by a stepwise washing of the complex with an oil fraction, decomposition of the complex with the release of paraffins, characterized in that, in order to increase the yield of paraffins and the improvement of its quality, t at a temperature corresponding to the temperature of crystallization of a solution of urea. Dewaxing conditions Initial complexing temperature, ° С6060604473 The final temperature of complexing / С3535351948 Dilution of the reaction mixture extract solution The amount of extract solution by feeding Mogoss Wash Stages, May. % on raw materials7582.1) 83,282,281.3 Mixing time, min 55555 The temperature of the reaction mixture, S3535353535 Separating the deparafinate solution from complex The temperature of the deparafinate solution at its separation from the complex, ° С3535353535 Amount of separated deparafinate solution, May.% For raw materials 123,5129,5130,2130,7129,1 Washing the complex I stage of washing the complex Amount of the extracted thief (Fr. 150-200 ° C) from the second stage of washing the complex, May. raw materials 85 85 85 8585 The amount of alcohol in the extract solution, May.13 3131313 . Washing temperature of the complex, ° С3535353535 The amount of the extract solution obtained after the first stage of washing, wt.%, On raw materials85,886,286,186,985,9 The amount of alcohol in the extract solution, nas1212,1) 12,312,912,1 Stage II washing the number of regenerated leaching fraction (150 - 200 ° l) supplied to II wash step, sat.% of raw material8382,963,282,982.8 The amount of alcohol in the wash fraction, May.% 1312,813,113,1 2,9 The temperature of the washing complex, S3535353535 The amount of the extract solution supplied to stage I of the rpm / b complex, wt.Ј for raw materials8585,285,18585 The alcohol content in the extract solution, may.% 1313,213,113,213 Stage III washing of the complex The amount of the washing fraction is 100 - 1) 0 ° С, unsaturated with alcohol and supplied to the third stage of the washing of the complex, May. on raw material5050505050 The flushing temperature of the complex, ° C) 252623665 The amount of the extract solution obtained from the third stage of washing and aimed at diluting the reaction mixture without continuation of the table