SU1301840A1 - Method for dewaxing and deoiling petroleum products - Google Patents

Abstract

The invention relates to methods for the dewaxing and de-oiling of petroleum products using dehydrated solvents and can be used in the oil refining industry. The method solves the problem of drying a wet solution of a concentrate of solid hydrocarbons before removing the solvent from it, reducing the impurities of water and oil in the regenerated solvent, improving the performance of the dewaxing and de-oiling processes. The method includes the following stages: mixing the wet raw material with a solvent, cooling the mixture, separating solid hydrocarbons and ice from the dewaxed product by filtration, heating the solid products and separating the solid hydrocarbon concentrate and water with a mixture of solvent into the sludge to dissolve the dried concentrate solid hydrocarbons and dewaxed petroleum products. The essence of the invention is that a dried concentrate of solid hydrocarbons in an amount of 2.5-30% by weight, calculated on the products of this stage, is introduced into the separation stage of the sludge before the regeneration system. The use of the invention by comparison with known methods allows to dry the wet solution of solid hydrocarbons with a concentration of 0.33-1.02 wt.% Of water to a residual moisture concentration of 0.09-0.12 wt.%, To reduce the content impurities of the oil product in the regenerated solvent to 0.08–0.21 wt.%; reduce the water concentration in the regenerated solvent from 0.42–1.22 to O, 17–0.19 wt.% without using special drying equipment. The use of a solvent with a reduced content of oil and water impurities allows reducing the oil content in concentrates of solid hydrocarbons by 0.3-2.6 wt.%, Increasing the yield of dewaxed oils by 1.6-3.1 wt.%, Increasing the filtration rate of suspensions. by 7.6-15.2%. 1 tab. oo 00 4

Description

and sent to a settling tank, where a stream of apoMaTH4ecK iM enriched component of the watered solvent is simultaneously fed from the final evaporation steps of the solvent from solutions of dewaxed products and solid hydrocarbon concentrate.

To dehydrate the wet solution of solid hydrocarbon concentrate

The invention relates to dewaxing methods and combined dewaxing and deoiling methods using dehydrated solvents and can be used in the oil refining industry.

The purpose of the invention is to increase the degree of drying of the concentrate of solid hydrocarbons and reduce the content of May-10 before removing the solvent in it, increasing the purity of the stanchion injects a stream of dried reconstituted solvent, or increasing the solid hydrocarbons to reduce the amount of dewaxed hydrocarbons. 2.5-30 wt.% For products, oils and increase in the filtration rate of suspensions, t5

The method is carried out as follows.

Raw materials (paraffin oil) are diluted with a solvent, which is used as a mixture of 50-70% ketone 20 (methyl ethyl ketone, acetone) and 70-50% of the aromatic component (toluene) and the filtrate solution of the second filtration stage. The raw suspension is cooled in crystallizers to form crystals of solid hydrocarbons and separated on vacuum filters of the first filtration stage at (-15) - (- 30) ° С (depending on the required temperature of solidification -30), which leads to the formation of two dewaxed oil). Osapas: a dried solution of a concentrate concentrate concentrate dock solid hydrocarbon concentrate is diluted with a dry solvent cooled in

The dried solid hydrocarbon concentrate, free from solvent impurities, is supplied to the settling tank from the last evaporation stage of the solvent. As a dried concentrate of solid hydrocarbons, slack or petrolatum dewaxing, paraffin or ceresin combined de-refining processes and de-oiling can be used.

The dried concentrate of solid hydrocarbons, fed to the sump, extracts additional quantities of solvent from a partially dried solution of a concentrate of solid hydrocarbon-solid hydrocarbons and a solution of water mixed with a solvent.

Introduction of dried concentrate

propane vaporizers up to a temperature of 35 solid hydrocarbons in the amount

filtration at the second stage, and divided into vacuum filters of the second stage,

If the process is carried out according to a combined dewaxing and deoiling process, the separation of the suspension is carried out in 3-5 filtration stages, and the temperature at all filtration stages should be such that the moisture entering the system with the raw material

The introduction of solid hydrocarbon concentrate in an amount of more than 30 May,% leads to a decrease in water and oil impurities in the regenerated solvent, however, increasing with

or from additional sources, it was retained on filters in the form of ice crystals, and its traces remained in the filtrates solution. The total multiplicity of dilution of the raw material, dissolving the energy consumption for circulation and the body, when separating suspensions into two more filtration stages that are no longer achieved, is held in an amount of 2.5-4 May, fractions, and when separating suspensions in 3-5 filtration steps, 3 , 5-6 May, a share. Sludge concentrate solid hydrocarbons and ice filters

process indicators (output of dewaxed oils, filtration rates, decrease in oil content in solid hydrocarbon concentrates) make it impractical.

The dried solution of the solid hydrocarbon concentrate is removed from the settling tank and sent to

the last stage is heated to the temperature of complete dissolution (40-60 ° C)

and sent to a settling tank, where a stream of apoMaTH4ecK iM enriched component of the watered solvent is simultaneously fed from the final evaporation steps of the solvent from solutions of dewaxed products and solid hydrocarbon concentrate.

To dehydrate the wet solid hydrocarbon concentrate solution

Before removing the solvent, a stream of dried concentrate of solid hydrocarbons in the amount of 2.5-30 wt.%, is introduced into the settler;

Before removing the solvent, a stream of dried concentrate of solid hydrocarbons in the amount of 2.5-30 wt.%, is introduced into the settler;

genera, which leads to the formation of two phases: a dried solution of the concentrate

The dried solid hydrocarbon concentrate, free from solvent impurities, is supplied to the settling tank from the last evaporation stage of the solvent. As a dried concentrate of solid hydrocarbons, slack or petrolatum dewaxing, paraffin or ceresin combined de-refining processes and de-oiling can be used.

The dried concentrate of solid hydrocarbons fed to the settling tank extracts additional quantities of solvent from the partially dried solution of the concentrate of solid hydrocarbons, which leads to the formation of two phases: a dried solution of the concentrate

solid hydrocarbons and a solution of water mixed with a solvent.

Introduction of dried concentrate

less than 2.5 wt.% does not allow to dry a wet solution of a concentrate of solid hydrocarbons, to reduce the content of impurities of oil and water in per. non-solvent solvent, reduce the oil content in the concentrates of solid hydrocarbons, increase the yield of dewaxed oils and increase the filtration rate.

The introduction of a concentrate of solid hydrocarbons in an amount of more than 30 May,% leads to a decrease in the impurities of water and oil in the regenerated solvent, however, increasing with

In this case, the energy consumption for circulation and the

In this case, the energy consumption for circulation and the

process indicators (yield of dewaxed oils, filtration rates, reduction of oil content in concentrates of solid hydrocarbons) make it impractical.

The dried solution of the solid hydrocarbon concentrate is removed from the settling tank and sent to

solvent in three stages of evaporation by supplying acute water vapor to the last stage of evaporation. The dry solvent from the first two evaporation stages is returned to the process. Watered solvent from the last evaporation stage is returned to the sump. Dry concentrate of solid hydrocarbons from the last stage

evaporation is directed to the fleet, fO of hot water vapor to the last

and part of it is introduced into a sump with a wet solution of a concentrate of solid hydrocarbons. The solution of dewaxed oil products (dewaxed oil, blind - vox) is directed to removal of the solvent in four stages of evaporation with the supply of sharp water vapor to the last Step, Dry solvent

From the first three stages of evaporation, 20 are poured into a product park. The content is added to the water-flooded process. The mixtures of the oil product and water in the solvent solution are fed from the last stage into the sump before the regeneration system. Dewaxed

the solvent recovered from the dried petrolatum solution is 0.08 and 0.15% by weight, respectively.

petroleum products from the last stage 25 The oil content in the petroleum precipitate of evaporation of the solvent is pumped to 18.2%.

commodity park. Example 2. 100 g raffinate fraction

A solution of water containing impurities of 350–420 ° C Stavropol oil of the submersible is sent from the sump before the regeneration system to the ketone column to remove the impurity and dissolve the dewaxing in two stages of 30 filtration in the presence of the solvent IEC – toluene (70:30% vol.) . The total dilution of the raw material with solvent is 1: 2.8 parts by weight; the filtration temperature in the first stage is

Dewaxing is carried out in two stages 30 of filtration in the presence of MEK-toluene solvent (70:30 vol.%). The total dilution of the raw material with solvent is 1: 2.8 parts by weight; the filtration temperature in the first stage is

ritel. The distillate of the column, in the form of an azeotropic mixture of ketone and water, is used to irrigate the column, the residue is fed into a settling tank before the system at minus 25 ° C, to the second - minus 23 C. regeneration. The water from the bottom ketone sediment of the solid hydrocarbon column concentrate is removed from the system.

reprocessing under the conditions described

Example 1. 100 g of residual example 1, except for the raffinate (fraction boiling above jg, then a stream of dried 490 ° C) is supplied to a settling tank with Ukhta oil subjected to dewaxing in two stages of filtration in the presence of MEK-toluene solvent (50:50 about .%) The total dilution of the raw material with a solvent of 45–420–500 C in West Siberia is 1: 4 mas. H, the temperature of the oil filter is subjected to deparaffinization at the first stage minus 28 ° C and at the second minus 25 ° C. A precipitate of a concentrate of solid hydrocarbons (petrolatum) and ice from the filters of the second Q. The supply of the raw material with a solvent of an amount of 120 g is heated to 1: 6 wt.h. The filter temperature is up to. 50 ° C and sent to a settling tank, where 45 g of watered solvent, obtained from the last stages of evaporation from solution of solid hydrocarbons (paraffin) from the dewaxed oil and third stage pet filters, are simultaneously subjected to rolatum. For dehydration of the wet, further processing under the conditions, the solution of petrolatum into the settling tank is described in Example 1, except for giving a stream of dried petrolatum in that a stream is fed into the settling tank.

30% .Mn.% gacha in the amount of products entering into the sump.

Example 3. YuOg raffinate

Cho,

de-oiling in three filtration steps in the presence of a solvent CK - toluene (60:40 vol.%). The total ratios in the first, second, and third stages are -28, -18, -10 ° C, respectively. Sediment concentrate

8404

the amount of 2.5 wt.% N and the products entering the sump. The resulting mixture is separated by two phases: a drained solution of petrolatum and a solution of water mixed with a solvent. The dried solution of petrolatum with a residual moisture content of 0.09% is directed to removing the solvent in three stages of evaporation with feeding

evaporation stage. The dried petroleum solvent free of impurities from the last stage of evaporation is sent to the inventory, and part of it is introduced into the sump as a circulating stream. The dewaxed oil after removing the solvent from it in four stages of evaporation in the amount of 66.8 wt.% Direct 350-420 From Stavropol oil under

Dewaxing is carried out in two stages of filtration in the presence of MEK-toluene solvent (70:30 vol.%). The total dilution of the raw material with solvent is 1: 2.8 parts by weight; the filtration temperature in the first stage is

minus 25 ° С, on the second - minus 23 C. The precipitate of solid hydrocarbon concentrate (gaucha) is subjected to further

 Example 1, except for the fact that a stream of dried fractions 420-500 C is supplied to the sump. West Siberian oil is subjected to dewaxing and the supply of solvent to the stock is 1: 6 wt.h. The temperature of the filter of solid hydrocarbons (paraffin) from the filters of the third stage is subjected to further processing under the conditions described in example 1, except for the fact that a stream is supplied to the sump

30% .Mn.% gacha in the amount of products entering into the sump.

Reamer 1, except for that, a drainage stream is supplied to the settling tank. 420-500 C West-Siberian is subjected to dewaxing and the raw material is diluted with a solvent of 1: 6 wt. The temperature of the filter ryh hydrocarbons (paraffin) from the third stage stages is subjected to the most processing under the conditions in Example 1, except that the stream is fed into the sump

Example 3. YuOg raffinate

Cho,

 of example 1, except for that, a stream of drying of 420-500 C of West Siberian oil is subjected to dewaxing oil and the supply of solvent by solvent is 1: 6 mas. The temperature of the filter-solid hydrocarbons (paraffin) from the filters of the third stage is subjected to further processing under the conditions described in example 1, except that a stream is supplied to the sump

de-oiling in three filtration steps in the presence of a solvent CK - toluene (60:40 vol.%). The total time of example 1, except for that, a stream of dehydration of 420-500 C is supplied to the sump of West Siberian oil and is subjected to dewaxing. The flow rate of the raw material is 1: 6 mph. The temperature of the filter-solid hydrocarbons (paraffin) from the filters of the third stage is subjected to further processing under the conditions described in example 1, except for the fact that a stream is supplied to the sump

The first, second, and third steps are -28, -18, -10 ° C, respectively. Sediment concentrate

dried paraffin in the amount of 15.8 wt.% on the products entering the sump.

Example 4, 100 g of residual raffinate (fraction boiling above 490 ° C) of Ukhta oil is subjected to dewaxing and deoiling in three stages of filtration in the presence of a solvent CK - toluene (50:50 vol.%) The total dilution of the raw material to solvents is 1: 8 ma.ch.

The filtration temperature in the first, second, third filtration stages is -28, -18, respectively. The precipitate of solid hydrocarbon concentrate (ceresin) from third-stage filters is subjected to further processing under the conditions described in Example 1, except that 2% by weight of dried ceresin is fed to the sump to the sump.

Example 5. 100 g of raffinate fraction 350-420 With Stavropol oil is subjected to dewaxing in two stages of filtration. The solvent used and the conditions are the same as in example 2, except that in the sump before the solvent regeneration system, a circulating stream of hatch is supplied in an amount of 35% by weight to the products entering the sump.

The main indicators of the proposed method in comparison with the known are shown in the table.

Examples by a known method carried out on the same raw materials as the corresponding examples of the proposed method.

Claims (1)

Invention Formula The method of dewaxing and deoiling of petroleum products by mixing wet raw material with a solvent, cooling the mixture, separating solid hydrocarbons and ice from the dewaxed product by filtration, heating solid products, separating solid hydrocarbons and water with a mixture of solvent into a wet solution, followed by solvent recovery that is different the fact that, with the aim of increasing the degree of drying and reducing the oil content in the concentrate of solid hydrocarbons, increasing the purity of the regenerants nnogo solvent dewaxed oil and increasing the filtration rate at the step of separation of sludge injected dried solid hydrocarbons concentrate in an amount of 2.5-30 wt.% based on the products of said step. 50:50 70:30 60:40 50:50 70:30 2,530,018,5 2.0 35.0 0,090,120,11 0,220,09 0,150,190,17 0,31 0.18 Editor S. Pekar Compiled by L. Ivanova Tehred V. Kadar Proofreader and. Erdein Order 1191/26 Circulation 464 VNSHSHI USSR State Committee for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5 Production and printing company, Uzhgorod, st. Project, 4 50:50 70:30 60:40 2.0 35.0 0.33 1.02 0.59 0.18 0.42 1.22 0.74 Subscription