RU99779U1 - DEVICE FOR PROCESSING APPARATUS OIL GASES - Google Patents

Abstract

The utility model relates to the oil and gas industry, in particular to systems for the utilization and use of associated petroleum and raw natural gases in the energy sector. A device for processing associated petroleum or raw natural gases by catalytic conversion for further use, for example, in public utilities or for transport via gas pipelines, consists of a start-up system, a feed and dosing system of reagents, a converter, heat exchangers, a control system, a catalyst is installed in the converter , which allows converting carbon-containing compounds into methane present in associated petroleum and raw natural gases. The technical result - the possibility of efficient utilization and beneficial use of associated petroleum or raw natural gases in the household, including through transport through gas pipelines to the end consumer. 1 n.p., 9 z.p. f-ly, 1 ill.

Description

The utility model relates to the oil and gas industry, in particular to systems for the utilization and use of associated petroleum and raw natural gases in the energy sector.

When oil is extracted during the separation process, a large amount of associated petroleum gas (APG) is dissolved in it. They are a mixture of gaseous hydrocarbons of various molecular weights, mainly subdivided into methane and the so-called broad fraction of light hydrocarbons (NGL). These associated gases, having a high energy content, are a valuable energy source. One of the effective and technologically advanced options for the utilization of associated petroleum gases is the generation of electric and thermal energy using, for example, gas reciprocating power plants directly at the oil field. However, this method is directly applicable only to fields with a stably high (75% and higher) methane content and low NGL content. Many well-known deposits contain significantly lower amounts of methane with a high content of NGL, causing detonation and failure of gas reciprocating stations based on internal combustion engines or exceeding the allowable level of toxic components in the exhaust gases of gas turbine plants. A separate problem is the inconstancy of the composition of APG, which can be subject to significant fluctuations over time, sometimes even during the day. One of the possible APG utilization approaches currently known is fractionation (for example, by separation at low temperatures, compression at high pressures, separation on membrane filters or by adsorption processes) into methane suitable for generating electric and thermal energy, and BFLH, used as a raw material for the chemical industry. Since this process is economically justified only in gas refineries, oil companies are faced with the need to invest heavily in the creation of gas transmission and processing facilities. The construction of such an infrastructure is economically efficient only in large fields and economically unreasonable in medium and small fields. In principle, the above also applies to raw, that is, untreated, natural gases, in which the proportion of NGL can also be quite high.

One of the promising approaches for the use of associated petroleum gases is also its transfer to nearby settlements, which has an acute problem of energy supply. However, the transmission of associated petroleum gas without preliminary preparation through the main gas pipeline to nearby settlements to meet household needs is also fraught with a number of difficulties caused primarily by condensation of BFLH and blockage of pipes. Moreover, associated petroleum and natural gases supplied to the main gas pipelines must comply with the requirements of OST 51.40-93 “Natural combustible gases supplied and transported through main gas pipelines”. As a result, the oil and gas production fields cannot channel the associated or raw gases they produce for the needs of the population living in the neighborhood, whose energy needs are met by using expensive imported fuel, which is often delivered to remote oil production areas only seasonally.

To solve this problem, associated petroleum and raw natural gases are prepared for transport via gas pipelines. The methods used are mainly based on the separation of methane from other components contained in the APG. A common drawback of all known methods of preparing APG and raw natural gases for transportation is the need for the subsequent disposal of BFLH components, which without proper processing or transportation will accumulate in the field. Moreover, the majority of existing methods, with all their attractiveness, have their own drawbacks that do not allow their application in practice.

For example, a method is known for removing higher hydrocarbons from natural associated petroleum gases (RU 2218979, B01D 53/22, B01D 71/70, 12/20/2003), which is based on the supply of a shared mixture of hydrocarbon gases from one side of a selectively permeable membrane and the selection of penetrated through her heavier components of the mixture with the other. The disadvantage of this method is the insufficient degree of separation of the components.

A known installation and method of processing associated petroleum gas by low-temperature condensation (RU 2340841, F25J 3/02, B01D 5/00, 10.12.2008). The method includes the compression of the source of petroleum associated gas, its cooling and separation to obtain dry gas and gas condensate. The disadvantages of this method is the high investment and energy costs due to the presence of a large number of compressors, separators, the need to use a cold source.

Also known is a method of separating C ₃₊ hydrocarbons from associated petroleum gases (RU 2338734, C07C 7/11, 20.11.2008) by countercurrent absorption by the absorbent, followed by desorption of the absorbed C ₃₊ fraction, and returning the absorbent regenerated after desorption to the absorber. The disadvantage of this method is not deep enough for transport in the gas pipeline gas purification from liquid fractions and the need for periodic regeneration.

A known installation for the preparation of natural and associated petroleum gas for transport (RU 2336932, B01D 53/00, F17D 1/02, 10/27/2008), equipped with a gas separator, which makes it possible to separate propane and isobutane in the form of gas hydrates, while methane and ethane sent to the gas receiving unit. The disadvantage of this method is the formation of gas hydrates of compounds With ₃₊ , also requiring subsequent disposal.

A known method (RU 2130961, C10G 35/04, 05/27/1999) of processing a wide fraction of light hydrocarbons and associated petroleum gases into highly aromatic liquid hydrocarbons by evaporation and heating of the feed in the furnace, contacting it with a zeolite-containing pentasil group catalyst located in a system of series-connected stages catalyst reactors with interstage heating of raw materials, separation of reformate into target products, and catalyst regeneration by burning coke. The disadvantage of this method is the high capital costs of the process and low demand for the resulting highly aromatized liquid hydrocarbons.

There is a method of preparing associated petroleum and raw natural gases for use in reciprocating internal combustion engines (RU 2385897, C10L 3/10, F02M 31/00, 04/10/2010), which consists in preparing the gas in a mixture with an oxygen-containing gas, for example with air, subjected to heat treatment at a temperature of 450-1100 ° C for 0.01-50 s with a free oxygen content in the mixture of 0.5-5%. Heat treatment can also be carried out in the presence of catalysts for oxidative condensation of methane, steam, carbon dioxide conversion of methane, oxidative dehydrogenation of lower alkanes, or a combination thereof. Nitrogen oxides, hydrogen peroxide, halogen compounds, unsaturated or oxygen-containing hydrocarbons, or reducing the likelihood of soot formation (water vapor) can act as reaction promoters. As a result, under the indicated conditions, the conversion of lighter C ₁ -C ₄ hydrocarbons is practically not observed, while the conversion of C ₅₊ hydrocarbons having very low methane numbers exceeds 95%. The main products of the conversion of C ₅₊ hydrocarbons during such heat treatment of associated petroleum gases are (in decreasing order of yield) ethylene, methane, ethane and carbon monoxide. The disadvantage of this method is the lack of conversion of the C ₂ -C ₄ component of associated petroleum gas, which does not allow its use for transporting the produced gas through gas pipelines.

The utility model allows us to solve the problem of efficient processing of associated petroleum or raw natural gases for the purpose of subsequent use, for example, for further transportation through gas pipelines.

The problem is solved through the use of a device for processing associated petroleum or raw natural gases by catalytic conversion to methane, as well as using the method of its operation. In addition to methane, for example, small amounts of hydrogen can be formed as conversion products. Its presence when using methane in the future, for example, to power power plants, improves the efficiency of a power plant and reduces harmful emissions into the atmosphere. By changing the parameters of the catalytic conversion, it is possible to carry out targeted regulation of the amount of hydrogen in the mixture in accordance with OST 51.40-93 “Natural combustible gases supplied and transported through gas pipelines”.

The proposed device for the processing of associated petroleum or raw natural gases by catalytic conversion consists of a start system, a feed and dosing system for reagents, a converter, heat exchangers, and a control system. At least one catalyst bed is installed in the converter, allowing at a temperature not exceeding 450 ° C to convert carbon-containing compounds present in associated petroleum and raw natural gases to methane. One of the main purposes of the device is to process associated petroleum or raw natural gases for use in public utilities, including for transportation through gas pipelines.

A converter is located in the converter, the active component of which is used various combinations of aluminum oxides, silicon, transition and rare-earth elements of 4-6 periods, mainly of the fourth and fifth periods, mainly Cu, Co, Ni, Fe, Cr, Mn, Ti Zr; La, Ce, Y, Sm, Pr, Gd, and platinum group metals, mainly Pt, Pd, Rh, Ir, Ru, mainly Pt, Rh, Ru.

The catalysts installed in the converter in several layers can have different or the same composition.

The catalyst located in the converter may be a reinforced porous material made in the form of flat and corrugated gas-permeable reinforced tapes, combinations of which form gas-permeable catalytically active channels of various shapes and geometries.

The catalyst may be in the form of blocks on a metal, ceramic or cermet support. The metal, ceramic or ceramic-metal support for the catalyst can be a direct channel block, including microchannel, block material with a complex configuration of channels and foam.

The catalyst may take the form of granules of various shapes and geometries.

In the start-up system of the device according to the invention, it is possible to use a heater, for example, an electric or flame heater operating on air and fuel, including associated petroleum or raw natural gas, or a heater-heat exchanger into which a heat carrier or any combination thereof is supplied.

The start-up system, the reagent supply and dosing system, the converter, the heat exchangers, the control system are separate structures or can be integrated with each other.

Heating or evaporation of the reagents supplied to the device, as well as controlling the temperature of the converter, is carried out using an electric heater or a flame heater, or by recovering the heat of the gases leaving the converter or by contact with the coolant, or any combination thereof.

The design of the reagent supply and dosing system in the device allows, if necessary, preheating or evaporation of the reagents before being fed to the start-up system and / or converter.

The design of the device, including the materials from which the device is made, allows conversion in the presence of oxygen-containing compounds, for example, water vapor and / or carbon dioxide, and / or oxygen and / or air.

The reagent supply and dosing system in the device allows oxygen-containing compounds, for example, water vapor or carbon dioxide, or oxygen, or air, or any mixture thereof in various quantities, to be supplied to any of the catalyst layers in the converter.

To obtain the maximum methane yield with a minimum volume of the device for any catalyst layer in the converter, a certain spatial distribution of the temperature profile can be established, for example, any catalyst layer can be both in isothermal conditions and in the conditions of a temperature gradient across the layer.

The design of the device allows the conversion of associated petroleum or crude natural gases at a pressure above atmospheric.

In addition to methane, the conversion products can be, for example, hydrogen and / or carbon monoxide and / or carbon dioxide, while the hydrogen content in the conversion products can be controlled so that its amount does not exceed 10 vol.%, Mainly does not exceed 3 about.%.

The start-up of the device is carried out using a heater, for example, an electric or flame heater operating on air and fuel, including associated petroleum or raw natural gas, or a heat exchanger to which the coolant is supplied, or any combination thereof.

Before feeding into the start-up system and / or converter, if necessary, preliminary heating or evaporation of reagents is carried out. Heating or evaporation of the reagents, as well as controlling the temperature of the converter, can be carried out using an electric heater or a flame heater, or by recovering the heat of the gases leaving the converter, or by contact with a coolant, or any combination thereof.

Catalytically converted associated petroleum or raw natural gases can be used, for example, in public utilities, including transported through gas pipelines.

A distinctive feature is the use of a catalyst in the device, which allows converting carbon-containing compounds present in associated petroleum or raw natural gases to methane at temperatures not exceeding 450 ° C. A device for processing associated petroleum or raw natural gases by catalytic conversion, in addition to converter 8, includes a start-up system 5, a supply and dosing system for reagents 2, heat exchangers 4, and a control system 9 (Fig.).

Structurally, the start-up system 5, the feed and batching system of reagents 2, the converter 8, the heat exchangers 4 and the control system 9 can be either separate parts of the device or can be integrated with each other.

As a converter, a catalytic reactor is used, containing one or more layers of catalysts 7, which provide the conversion of associated petroleum or crude natural gases to methane. The catalysts in the catalytic reactor can be placed in the form of granules of various shapes and sizes, blocks and foam with a system of gas-permeable channels. To improve thermal conductivity, the catalysts can additionally be applied to a metal, ceramic or cermet carrier. This carrier can be formed into a structure containing a system of channels (including microchannels) of various geometries and configurations providing gas permeability through a catalytic unit.

The start-up system 5 uses an electric heater 6. At start-up, the converter can be warmed up by passing electric current directly through the electrically conductive elements of the catalyst. In the start-up system, a flame heater operating on air and fuel, including associated petroleum or raw natural gas, can be used, in addition, a heater-heat exchanger can be used, in which a coolant with the required temperature is supplied.

The heating or evaporation of the reagents, as well as the temperature control of the converter, is carried out using an electric heater 3 and 6. This can also be done using, for example, a flame heater, by recovering the heat of the gases leaving the converter, contact with the coolant, or a combination thereof .

As an example, in FIG. The proposed device for the catalytic conversion of associated petroleum or raw natural gases for use in power plants in conjunction with the main systems that ensure its operation is schematically depicted.

One of the options for the method of operation of the device is as follows.

To start the device for catalytic conversion of associated petroleum or raw natural gases, associated petroleum gas APG, and oxygen-containing compounds 1 (for example, air), using the supply and metering system 2, which includes the corresponding devices, is supplied to the system through an electric heater 3 and a heat exchanger 4 launch 5, combining the functions of a heat exchanger. For the initial heating to the desired temperature of the converter 8 containing the catalyst layers 7, for example, flame combustion of the supplied APG is performed. At the same time, hot reaction products formed as a result of complete oxidation (carbon dioxide and water vapor) passing through heat exchanger 4 can also preheat or evaporate reagents (APG and oxygen-containing compounds). Preheating of APG and oxygen-containing compounds can be carried out not by an electric, but by a flame heater 3, when, for example, part of the supplied APG is burned, thereby heating the bulk of the reagents supplied to the launch system. Preheating of APG and oxygen-containing compounds, as well as heating of the converter 8 containing catalyst layers 7, can be carried out using an electric heater 6, as well as any hot coolant GT.

After the catalyst 7 reaches a temperature at which it is possible for the catalytic conversion of APG to occur, for example, 400 ° C, the start-up system 5 and converter 8 are transferred to the APG conversion mode. To do this, using the supply and metering system 2, APG and oxygen-containing compounds (for example, water vapor) 1, preheated in the heat exchanger 4, are fed to the converter 8, where, upon contact with the first catalyst bed, a catalytic conversion takes place. If the heat exchanger 4 provides sufficient preheating of the APG and oxygen-containing compounds, then the electric heater 3 may not be involved. To optimize the conditions of the catalytic reaction (for example, maintaining a given temperature, the complete conversion of carbon-containing compounds), an additional amount of oxygen-containing compounds is fed to the second catalyst bed. In this case, the temperature of the catalyst layers is controlled in such a way that the temperature decreases in the direction of the reaction mixture in the converter, for example, the first catalyst layer is isothermal at a temperature of 350 ° C, and a temperature gradient of 350 ° C at the inlet is set for the second catalyst layer to 250 ° C at the exit. Further, converted CNG associated petroleum gas, consisting mainly of methane and containing small amounts of hydrogen (~ 5 vol.%), Passing through heat exchanger 4, can be used for its intended purpose (in public utilities, transported via a gas pipeline). If necessary, an excess of unconverted oxygen-containing compounds can be removed from the CNG. To maintain the optimum temperature profile in the converter, a certain part of the CNG before passing through and a certain part of the CNG after passing through the heat exchanger 4 is passed through the start-up system 5 through the start-up system 5, which in this case already acts as a heat exchanger. Further, CNGs can also be used for their intended purpose (in public utilities, to undergo transport through the main gas pipeline). To control the temperature in the converter, an electric heater 6 can be used.

To carry out preheating of APG and oxygen-containing compounds, to regulate the temperature in converter 8, a hot coolant GT can also be used, for which its predetermined amount is passed through heat exchanger 4 and start-up system 5, respectively.

In the case of the process at a pressure above atmospheric, the device can be made in a more compact design and its specific productivity for converting APG is increased.

The start-up and operation of the device, as well as all related systems, are controlled using a microprocessor system (control system) 9. Such a microprocessor system can operate both autonomously and in conjunction with other related electronic systems.

The considered example does not show and does not limit all possible options for implementing the design of the device for processing the catalytic conversion of associated petroleum or raw natural gases into methane.

The proposed device allows you to effectively convert associated petroleum or crude natural gases into methane, thereby removing carbon components other than methane containing components having a high boiling point.

The main advantage of the device is the possibility of using the energy contained in associated petroleum gas for domestic needs, which allows without the creation of additional expensive infrastructure to involve associated gases that are uselessly burned to date in most oil fields.

Claims (10)

1. A device for processing associated petroleum or raw natural gases by catalytic conversion, consisting of a start-up system, a reagent supply and dosing system, a converter, heat exchangers, a control system, characterized in that at least one catalyst layer is installed in the converter, allowing at a temperature not higher than 450 ° С, convert carbon-containing compounds to methane present in associated petroleum or raw natural gases. 2. The device according to claim 1, characterized in that the converter contains a catalyst, the active component of which is used various combinations of oxides of aluminum, silicon, transition and rare earth elements of 4-6 periods, mainly the fourth and fifth periods, mainly Cu, Co Ni, Fe, Cr, Mn, Ti, Zr; La, Ce, Y, Sm, Pr, Gd, and platinum group metals, mainly Pt, Pd, Rh, Ir, Ru, mainly Pt, Rh, Ru. 3. The device according to claims 1 and 2, characterized in that the catalysts installed in the converter in several layers can have different or the same composition. 4. The device according to claims 1 and 2, characterized in that the converter contains a catalyst, which is a reinforced porous material made in the form of flat and corrugated gas-permeable reinforced tapes, combinations of which form gas-permeable catalytically active channels of various shapes and geometries. 5. The device according to claims 1 and 2, characterized in that the converter has a block catalyst on a metal, ceramic or cermet carrier. 6. The device according to claims 1 and 2, characterized in that in the converter the metal, ceramic or ceramic-metal support for the catalyst is a direct channel unit, including microchannel, block material with a complex configuration of channels and foam. 7. The device according to claims 1 and 2, characterized in that the catalyst is located in the converter in the form of granules of various shapes and geometries. 8. The device according to claim 1, characterized in that the start-up system uses a heater, for example an electric and / or flame heater, operating on air and fuel, including associated petroleum or raw natural gas, and / or a heat exchanger into which hot heat carrier is supplied. 9. The device according to claim 1, characterized in that the start-up system, the feed and dosing system of the reagents, the converter, the heat exchangers, the control system are separate structures or can be integrated with each other. 10. The device according to claim 1, characterized in that the heating or evaporation of the reagents, as well as the temperature control of the converter, is carried out using an electric and / or flame heater, and / or due to heat recovery of the gases leaving the converter, and / or by contact with coolant.