The method of extraction of benzene hydrocarbons from coke oven gas

 

(57) Abstract:

The inventive coke oven gas is treated in the absorber light coal oil. The absorbed benzene hydrocarbons are distilled. Obtention oil assign for treatment of polymer products in the amount of 1.5 to 5.0 wt.% from the time oil consumption and absorption, mixed with aliphatic hydrocarbons, wikipedii within 60 to 120°C. in a volume ratio of aliphatic hydrocarbons and oils, equal to (2 - 5): 1. The oil mixture with the aliphatic hydrocarbons are separated from the formed precipitate the polymer product by decantation. Aliphatic hydrocarbons are removed by distillation. Peeled from the polymer products of the oil return into the cycle. Preferably, in the exhaust purification from polymer products obtention oil add coal tar mass ratio of oil and coal tar (1,5 - 5,0):1. 1 C.p. f-crystals, 3 tables.

The invention relates to the extraction of benzene hydrocarbons from coke oven gas by absorption of light coal oil, followed by separation from the circulating oil by distillation with water vapor and can be used in the process is

The method for extracting the benzene hydrocarbons from coke oven gas by absorption of light coal oil with subsequent distillation of a busy working oil with water vapor at a temperature of 135-180aboutAnd return obessessing oil after cooling again to the absorption of benzene hydrocarbons, as described in the technical literature. The disadvantage of this method is the high consumption of fresh absorbing oil for full or partial replacement of working capital due to higher viscosity and density of the latter due to the polymerization of unsaturated compounds and copolymerization of other components of coke oven gas and absorbing oil during its periodic heating and cooling.

The closest analogue of the present invention is a method of extraction of benzene hydrocarbons from coke oven gas by absorption of light coal oil with subsequent distillation of the oil at a temperature of 135-180aboutWith water vapor and the release of a portion of the circulating absorption oil polymers by distillation nepalitano faction and return it to the cycle of the circulating oil. The polymers are of the cycle of the circulating oil in liquid form is a private part of the oil, high loss of oil polymers limited number displayed for separating polymers circulating oil, which is limited by the flow of steam in the distillation column distillation of the benzene hydrocarbons from the circulating oil. For example, according to published data, when the number of circulating oil 136 m3/h in the regenerator is served only 0.4 t/h circulating oil from which Argonauts nepalitano faction only about 0,228 t/H. At the same time to maintain good quality recycling oil regeneration (highlighting polymers) must display at least 1.5% of the circulating oil.

If the regenerator output 1% of the working oil and the distillation polimernoi his part to serve the whole of acute water vapor supplied to a distillation column for distillation of circulating oil benzene hydrocarbons, at a temperature of 170aboutWith regenerator otnosyatsa 79.5% of oil. If there are no plants to water vapor high oil regeneration (highlighting polymers) is practically impossible, and in practice, the plants have to apply the update working oil to the simple conclusion it from circulation and replaced by fresh, which leads to increased oil consumption th adsorption of coal oil, reducing the consumption of fresh replenishment cycle and the possibility of using low-grade heat transfer fluids.

This objective is achieved in that the selection of polymers by mixing the output from the cycle of the circulating oil with an aliphatic hydrocarbon wikipedie within 60-120aboutWith in a volume ratio of aliphatic hydrocarbons oil within 2-5, followed by decantation of the layer of oil hydrocarbons and distillation of aliphatic hydrocarbons by distillation.

To significantly improve the quality of the circulating absorption oil for separation of polymers from the series output of 1.5-5% of time flow rate of the circulating oil.

To reduce the consumption of fresh oil on the replenishment cycle of working to be displayed on the selection of polymers circulating oil is added coal tar mass ratio of oil and resin in the range of 1.5-5.

P R I m e R 1. The flow of coke oven gas 100 thousand m3/h with the content of benzene hydrocarbons 40 g/m3washed in the absorbers in a counter light coal oil density 1050 kg/m3and a viscosity of 1.5aboutE (6,74 cSt), supplied in a quantity of 180 m3/hours After absorption benzoe distillation of him benzene hydrocarbons. Obtention absorbing oil after distillation column is cooled to 25-30aboutS and 9 m3/h assign to selection of polymers, and 171 m3/h mixed with 0.20 m3/h fresh absorbing oil and 8.8 m3/h regenerated and again served on the absorption of the benzene hydrocarbons.

To maintain constant density and viscosity 9 m3/h output from the cycle of the circulating oil is mixed with 27 m3/h aliphatic hydrocarbons (benzene boot). After settling of the mixture deposited polymers pumped in coal tar, and the upper layer of solution adsorption of oil in the gasoline is fed to the column for distillation of gasoline at a temperature of 140aboutC. warded off petrol vapours condense and return to the mixing with the output of cycle 9 m3/h circulating oil, and obezbecivanje regenerated absorbing oil in the amount of 8.8 m3/h after cooling to 25-30aboutWith mix with the main stream of the circulating absorption oil supplied to the absorption of the benzene hydrocarbons from coke oven gas. To compensate for the loss absorbing oil in the cycle continuously add fresh light coal oil gas amounted to 2.2 g/m3and production of crude benzene 3890 kg/h

P R I m m e R 2. The flow of coke oven gas 100 thousand m3/h with the content of benzene hydrocarbons 40 g/m3washed in the absorbents in a counter light coal oil density 1064 kg/m3and a viscosity of 1.6aboutE, submitted in the amount of 180 m3/PM

After washing the gas saturated benzene hydrocarbon oil served on a distillation column for distillation of him benzene hydrocarbons at a temperature of 145aboutWith the supply of acute water vapor 9.6 t/h Obtention oil after distillation column is cooled to 25-30aboutS and 9 m3/h assign to selection of polymers, and 171 m3/h mixed with 9 m3regenerated and again served on the absorption of benzene hydrocarbons from coke oven gas.

To maintain constant density and viscosity of the working oil 9 m3/h output from the cycle oil mixed with 1.8 m3/h coal tar and 30 m3/h gasoline. After settling deposited polymers with a heavy part of the coal tar is directed to a Stripping cube and after the distillation of gasoline pumped into marketable coal tar or processed by WPI is the distillation of gasoline at a temperature of 140-150aboutC. In the same column and assign the pairs of Stripping cube for Stripping polymer. Distilled petrol vapours condense and return to the mixing with the new portion of the circulating absorption oil and coal tar, and uparennoe from gasoline absorbing oil in the amount of 9 m3/h mixed with 171 m3/h working capital and serves on the absorption of benzene hydrocarbons from coke oven gas. In this mode of regeneration circulating oil loss benzene hydrocarbons from the coke gas was 2.4 g/m3, production of crude benzene 3910 kg/h, and fresh oil for replenishment cycle, the reverse was not required.

To confirm the possibility of use as selective solvents aliphatic hydrocarbons of different molecular structures, or mixtures thereof described experiments, the results of which are given in table. 1.

In all experiments, the volumetric ratio of oil and solvent is maintained equal to 1 2. The source of circulating oil had a viscosity of 3aboutE and density 1096 kg/m3.

To select the optimal volume ratio of oil and solvent is conducted experiments with circulating absorption oil with the initial viscosity of 3.2aboutE and density 1098 kg/m

To verify the optimality of the selected ratio of coal tar and displayed on the selection of polymers oils experiments with handling gasoline type "boot" of the mixture circulating absorption oil with the source density 1096 kg/m3and a viscosity at 30aboutWITH, 2,6aboutE (16,6 cSt).

After decanting the top layer of the oil solution of gasoline and distillation of gasoline was determined output absorbing the regenerated oil, its density and viscosity at 30aboutC. the results of the experiments are given in table. 3.

Thus, from table. 1 shows that for the selection of the polymers of the circulating absorption oil can be used aliphatic hydrocarbons of various molecular structures including their mixtures and commercial gasoline direct the accomplishing of oil, and of the table. 2 shows that at a volume ratio of solvent and oil less 2 output the regenerated oil is sharply reduced, and the quality metrics "viscosity and density decrease. When the ratios of solvent to oil is greater than 5, the output and the quality of the recycled oil is virtually unchanged and increasing the consumption of solvent is meaningless.

Regarding the choice of solvent for temperatureoperating fluids, and difficulties in the use of more low-boiling aliphatic hydrocarbons (pentane and propane-butane fractions) due to the necessity of applying pressure or low temperature to prevent loss of solvent.

From table. 3 shows that the addition of coal tar to the circulating oil before allocation of a polymer with maintaining mass relationship of oil to the resin is less than 1.5 not only leads to increased viscosity and density of circulating the regenerated oil, but also leads to the formation of excess oil.

The higher the ratio of oil to resin over 5 virtually no effect on the quality of the recycled oil, but at the same time increases the need for fresh oil, because of the resin in this case is compensated only 3.5 wt. displayed on the regeneration oil 100, and you must make up 28.5% of 100.

Search according to the present invention, the criterion of novelty and "significant differences" showed that in the technical and patent literature are not described methods of extraction of polymers from absorbing coal oil by mixing it with aliphatic hydrocarbons.

The literature describes methods for the enrichment of anthracene using Wye what I highlight asphalts from petroleum oils and polymeric substances from fats, however, these data do not provide a basis to relate your presentation of them to the prototype or analogs of the proposed method of selection of the polymers of the circulating absorption coal oil extraction process benzene hydrocarbons from coke gas due to the significant differences of the ingredients used extractants, conditions and goals of way.

Based on the foregoing and in accordance with p. 21 Statute on discoveries, inventions and rationalization proposals", and according to p. 52 Instructions EZ-1-74, p. 6.03 Instructions EZ-2-74 and advice of the Department of methodology of VNIIKP in the journal "Questions of invention", N 4, 1984, S. 62-64, the proposed method for the extraction of benzene hydrocarbons from coke oven gas by absorption of light coal oil, consisting in the allocation of a portion of the circulating oil polymers by mixing it with aliphatic hydrocarbons, separating a mixture of oil hydrocarbons from polymers by decantation, distillation of aliphatic hydrocarbons by distillation and returning the regenerated oil in circulation, and hydrocarbon mixture with a new portion of the circulating oil, meets the criteria of "novelty" and "significant differences".

Aktalnye the extraction mode of the benzene hydrocarbons in the absence of heating steam high settings. The economic effect is determined by reducing consumption (losses) of an absorption oil, which is removed from the loop without Stripping the lungs straps with their return in the circulating oil.

Practice shows that in the absence of heating steam pressure 9-10 ATM flow adsorption of oil increases from 100 kg up to 200-300 kg per 1 ton of produced crude benzol.

At the same time offer a way of separating polymers from recycled oil can improve its quality and thereby reduce the loss of benzene hydrocarbons from the coke gas with 4-5 g/m3when absorbing the oil of poor quality to 2-2,5 g/m3.

1. The METHOD of extraction of BENZENE HYDROCARBONS FROM COKE oven GAS by absorption of light coal oil, followed by separation of the absorbed benzene hydrocarbons by distillation, removal of any resulting obessessing oil for treatment of polymer products and returning purified from the polymer products of oil in the loop, wherein for removal of polymer products obtention oil disperses in the amount of 1.5 to 5.0 wt. from the time oil consumption on the uptake and clearance from the polymer products is carried out by mixing from the practical hydrocarbons: oil 2-5:1, followed by the separation of the mixture of oil and aliphatic hydrocarbons from the resulting precipitate the polymer product by decantation and removal of aliphatic hydrocarbons by distillation.

2. The method according to p. 1, wherein the exhaust purification obtention oil add coal tar mass ratio of oil: coal tar pitch of 1.5 to 5.0:1.

 

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