The method of obtaining aromatic hydrocarbons from a gaseous mixture of light hydrocarbons containing propane and butane

 

(57) Abstract:

Usage: petrochemistry. Essence: the extraction of aromatic hydrocarbons from a gaseous mixture of light hydrocarbons containing propane and butane, includes condensation and absorption of at least part of the components of the material during its ejection liquid hydrocarbon stream, the stabilization of the obtained liquid mixture of hydrocarbon raw materials and active flow ejector emitting a mixture of hydrocarbons WITH4-and circulating active flow ejector, the contact mixture of hydrocarbons WITH4-with catalyst dehydrocyclization in terms of dehydrocyclization with obtaining product stream containing aromatic hydrocarbons, and the allocation of the flow of products of aromatic hydrocarbons. Effect: receiving a compressed raw materials without the use of compressors. table 2., 1 Il.

The invention will otnositsa a process for the production of aromatic hydrocarbons from aliphatic and may be used in the refining and petrochemical industry.

In the oil industry, oil and gas processing plants generates significant volumes of low-pressure gases containing components3+that can be used DL the key greenhouse gases need compression. The cost of compression of low-pressure gases are large and these gases are often burned at flares, resulting in the loss of hydrocarbons and deteriorate the environment.

In the patent literature describes numerous methods for obtaining aromatic hydrocarbons from light aromatic. In the reaction zone is usually served active in the reaction of dehydrocyclization hydrocarbons WITH2+and the reaction is carried out at elevated temperature and pressure.

There is a method /Pat. USA 4677235, 1967/ obtaining aromatic hydrocarbons from natural gas containing nitrogen, methane, ethane, propane and butane, in which methane, nitrogen and hydrogen are separated from the raw material and product in the area of the vapor-liquid separation, operating at a pressure of 2.8 MPa, the liquid flow in the zone of the fractionation produce a product stream containing hydrocarbons WITH the6+and a stream containing propane, and the last guide in the area of dehydrocyclization operating at pressures below 0.7 MPa. When this raw material is first compressed, then reduce its pressure, which can lead to loss of energy.

In a known way /Pat. RF 2139844, 1998, prototype/ obtaining aromatic hydrocarbons from petroleum gas in Ana1-C4, part of the vapor stream from the separation of the reaction products and the stream from the fractionation zone products containing propane and butane. When using raw, enriched WITH5+that reduce the stability of the action of the catalyst in the reaction zone is directed hydrocarbons WITH1-C4and noncondensable gases, selected in the zone of the fractionation of a mixture of raw materials and products. While hydrocarbons WITH5+raw materials are components of a stable product, a concentrate of aromatic hydrocarbons.

The latter circumstance is not always acceptable, therefore, require prior separation of the components5+from raw materials. Another problem is the compression of a gas of low pressure, enriched with hydrocarbons3+that requires speed compression when the pressure in the reaction zone can be increased with regular 0,7-1 MPa to 1.5-2 MPa to reduce the volume of the reactor when using diluted raw materials.

The use of compressors for compressing gases has some drawbacks: compressors roads, not enough reliable, require special services and facilities with a full system isaabah hydrocarbons solves the problem of obtaining without the use of compressors compressed raw material for the process of dehydrocyclization, contains the maximum number of components5+.

The method of obtaining aromatic hydrocarbons from a gaseous mixture of light hydrocarbons containing propane and butane, includes compression of raw materials, the contact of the compressed feedstock with a catalyst dehydrocyclization in terms of dehydrocyclization of raw materials to produce the product stream containing aromatic hydrocarbons, and the allocation of the flow of products of aromatic hydrocarbons, and differs in that the compression of the gaseous raw material is carried out using a liquid ejector by condensation and absorption of at least part of its components active stream of hydrocarbon liquid fraction to form a liquid stream containing components of raw materials and active flow ejector, the liquid stream is compressed by the pump and stabilize emitting compressed raw containing hydrocarbons WITH4-and flow of hydrocarbons FROM5+at least part of which is compressed and fed into the ejector as the active thread.

Gaseous raw material containing propane and butane, can be a mixture of hydrocarbons WITH1-C4that also includes components5+: associated gas, gases of all stages of oil separation obtained on the N raw materials at pressures of 0.1-0.7 MPa, containing components5+you want to retrieve. Raw materials may also include nitrogen, hydrogen, oxygen, oxides of carbon.

In a liquid ejector is compressed and liquefied mixture of light hydrocarbons by condensation and absorption of its active components flow, which is used as hydrocarbon fractions WITH5+petrol, diesel and other Active thread served in the ejector pressure in the preferred case up to 4 MPa.

Factors liquefaction of gaseous raw materials are compression ratio /pressure at the outlet of the ejector and the consumption of active thread /main absorbent medium. Flow active flow and its pressure is chosen so to obtain the desired degree of liquefaction of the raw material in the preferred case, at least 97% of components3+including full liquefaction. It should be noted that the catalytic processing of direct hydrocarbons, which when ejection of gaseous raw materials were orogeny.

Full liquefaction of the gaseous raw material can be achieved, when it does not include non-condensable components or their content is such that it allows full absorption of the active flow ejector. The EU preferred degree of liquefaction components3+at least 60%, taking into account the fact that their loss is inevitable during the separation of liquid phase from the vapor-liquid stream.

At the outlet of the ejector receive liquid or vapor-liquid mixture of hydrocarbon raw materials and active flow at a higher pressure than the feed mixture of light hydrocarbons. The pressure at the outlet of the ejector depends on the costs and pressures of active and commodity flows. The higher the pressure at the outlet of the ejector, the smaller the flow active flow required for liquefaction of the raw material and the higher the required compression of the active stream before entering the ejector.

The liquid flow from the ejector or the liquid phase selected in the separator of the liquid-vapor mixture of hydrocarbon raw materials and active flow, squeeze the pump until the pressure required to stabilize the mixture emitting a stream containing hydrocarbons WITH the4-raw material, which is used to produce aromatic hydrocarbons.

The stabilization of the liquid mixture of hydrocarbon feedstock and active flow stabilization is carried out in a column at a pressure of 1-2 MPa. From the top of the column output pair containing mainly hydrocarbons WITH1-C4and adjustable allowable number of hydrocarbons WITH5+5+the feedstock may be selected as a product. The hydrocarbons used as the active flow ejector, circulate in the system: the required number of them is compressed by the pump and sent to the ejector.

As a catalyst dehydrocyclization light hydrocarbons using known compositions of zeolites and metal promoters that increase the activity, stability and selectivity of zeolites.

The contact of the feedstock with the catalyst is carried out in conditions of dehydrocyclization components3+: usually when 650-450oWith that pressure of not more than 3 MPa, preferably 1-2 MPa, at a space velocity of the raw material 0,5-6,0 h-1.

The flow of the products formed upon contact of the feedstock with the catalyst, includes aromatic hydrocarbons, hydrogen, neprevyshenie raw material components, as well as methane and ethane, which are formed as by-products because of the low selectivity of the known catalysts. From the stream of products of known methods produce a concentrate of aromatic hydrocarbons and usually neprevyshenie hydrocarbons WITH3and C4for recycling.

The proposed pic is

The gaseous mixture of light hydrocarbons I in the ejector e ejection and absorb the active stream II. Coming out of the ejector flow III, representing the liquid or vapor-liquid mixture of hydrocarbon raw materials and active flow into the separator s-1, where, with partial liquefaction of the raw output of gas-phase stream V containing mainly his nscontainerframe and unabsorbed components. From the separator liquid stream IV pump N-1 is compressed to the desired pressure stabilization of the mixture, the resulting flow VI is heated in the heat exchanger T-1 and served in the stabilization column K. Hot irrigation columns are using reboiler T-2. From the top of the column output pairs (XI, cool them in the refrigerator for X and separator S-2 emit the condensed part as irrigation XII supplied to the column by the pump H-2, and a pair XIII from the separator containing hydrocarbons WITH1-C4gaseous raw materials come in the reactor block RB. The reactor block raw materials are heated and provide his contact with the catalyst dehydrocyclization in terms of dehydrocyclization with the formation of the product stream of the FOURTEENTH containing aromatic hydrocarbons, which emit in any known scheme. With necesto stable hydrocarbon fraction is compressed by the pump H-3 and the flow II served in the ejector as active, and the excess output from the set /thread IX/.

In table. 1 and 2 shows the main physical characteristics and hydrocarbon composition of the main streams in the scheme described in obtaining aromatic hydrocarbons /without extracting them from the mixture of products from a mixture of gases of low pressure at their full liquefaction in the ejector. As raw material for the process of dehydrocyclization get without using a compressor as a mixture of hydrocarbons1-C4when the pressure of 1.39 MPa. The catalyst dehydrocyclization has the following composition: zeolite NCWM group of pentelow with the content of sodium oxide to 0.12 wt.% and SiO2/Al2O3=35-68%; alumina - 30%; zinc oxide of 2 wt.%.

The method of obtaining aromatic hydrocarbons from a gaseous mixture of light hydrocarbons containing propane and butane, which includes compression of raw materials, the contact of the compressed feedstock with a catalyst dehydrocyclization in terms of dehydrocyclization of raw materials to produce the product stream containing aromatic hydrocarbons, and the allocation of the flow of products of aromatic hydrocarbons, characterized in that the compression of the gaseous raw material is carried out using a liquid ejector by condensation and absorption, contains the components of raw materials and active flow ejector, the liquid stream is compressed by the pump and stabilize with the release of the compressed feedstock containing hydrocarbons WITH4-and flow of hydrocarbons FROM5+at least part of which is compressed and fed into the ejector as the active thread.

 

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FIELD: organic chemistry.

SUBSTANCE: invention relates to synthesis of aromatic C-nitroso compounds. Invention describes new chemical compounds 1,3,5-trinitrosobenzene of the formula:

. Invention provides synthesis of new chemical compound that can be used in synthesis of dyes, antioxidants, polymer stabilizing agents and radical traps, and as an intermediate substance in organic synthesis and synthesis of medicinal preparations. 1,3,5-Trinitrosobenzene can be used as a vulcanizing agent of composition systems based on high-molecular compounds, for example, based on synthetic or natural rubbers, component of adhesion composites rubber-substrate.

EFFECT: valuable properties of compound.

2 dwg, 2 tbl, 3 ex

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