Method for coproduction of synthetic liquid hydrocarbons and methanol and plant for its implementation integrated into production train facilities of oil and gas condensate deposits

FIELD: oil and gas industry.

SUBSTANCE: method includes heating of source natural gas, mixing of superheated steam with source natural gas, one-stage conversion of gas and steam mixture in reformer to converted gas, cooling of converted gas and its division into two flows. The first flow is subject to one-stage catalytic conversion to methanol while the second flow is subject to catalytic synthesis with production of liquefied hydrocarbon gas which is sent to conversion together with source natural gas and liquid hydrocarbons subjected to stabilisation in rectification tower. Plant for implementation of the above method is suggested also in order to produce synthetic liquid hydrocarbons and methanol; the plant is integrated into production train facilities.

EFFECT: effective coproduction of methanol and synthetic liquid hydrocarbons in the same flow diagram during processing.

15 cl, 1 dwg

 

The invention relates to the sector of oil and gas processing and can be used to produce synthetic liquid hydrocarbons (SIU) and methanol on the unit integrated in the object field treatment of the gas, gas condensate and oil fields.

Development of hard-to-reach deposits already at the stage of construction and commissioning raises a number of issues related to the delivery of motor fuel and methanol. One way to solve such problems is the construction of the multi-function unit based on the technology of production of synthetic liquid hydrocarbons.

Currently, the method of obtaining SIU based on the Fischer-Tropsch process, is used as the only industrial method of obtaining liquid fuels from natural or associated gas without the intermediate formation of intermediates. The synthesis gas obtained by reforming of natural or associated gas, is converted directly into hydrocarbons.

Synthetic motor fuel received by such method have a good motor performance, environmentally friendly, because it does not contain sulfur, and nitrogen-containing polyaromatic compounds, but they are significantly more expensive than oil. The main disadvantage of the Fischer-Tropsch process is its low selectivity, mnogochislennye the researchers aim to increase the yield of liquid hydrocarbons.

Introduction industrial processes production of synthetic liquid hydrocarbons will allow oil and gas companies involved in the development of the vast reserves of gas, production of which was previously considered to be uneconomic due to the remoteness of the fields from gas consumers and the lack of transport infrastructure. So as to transport the liquid fuel is easier than gas. In addition, in areas of oil production on the torches burned a huge amount of associated gas. This causes significant damage to the ecology and economy of producing countries.

The optimal solution to this problem would be to place small plants for the processing of natural and associated gas into synthetic liquid hydrocarbons directly on the gas.

However, this raises a number of issues related to the technology of production of synthetic liquid hydrocarbon, as used in the synthesis of synthetic liquid hydrocarbon catalysts require a limited content of carbon dioxide in the original synthesis gas. As a result, when preparing the synthesis gas is separated and discharged into the atmosphere significant amounts of carbon dioxide, which could be used for the synthesis of methanol, widely used in the fields as an inhibitor hydrate is obrazovaniya.

A method of producing methanol, comprising steam reforming of methane to synthesis gas (mixture of CO and H2with its subsequent catalytic conversion to methanol (Karavaev M.M., Leonov V.E. and other Technology of synthetic methanol. - M.: Chemistry, 1984, p.72-125 [1]). The main disadvantages of this process: high demands on the purity of the source gas, and the high cost of energy for the production of synthesis gas and its clean, sophisticated equipment, a large number of intermediate stages of the process, the lack of profitability of small and medium enterprises with a capacity of less than 1000 tons/day.

Closest to the proposed is the installation for the production of methanol from natural gas and implemented them (for a utility model Patent of the Russian Federation No. 102537, published. 10.03.2011 [2]). Installation integrated in the installation of complex gas at the gas field and contains consistently installed and connected system piping heat exchangers for heating natural gas and gas-vapor mixture, the furnace reformer to obtain a converted gas; synthesis reactor for catalytic production of methanol from the converted gas and a separator, and a heat exchanger for heating the converted gas heat exchanger for heating the produced water, the HRSG to produce steam and the heat exchanger to superheat and the yield of pcs is reforming on the flue gas for use of heat is connected with the annular space of the heat exchangers for the natural gas heating, prepared water, overheated water vapor and heat the gas mixture, and a heat exchanger for heating the converted gas. The output of the reformer furnace in the converted gas is connected to the supply line of the converted gas to the synthesis reactor, sequentially passing through the HRSG, the annulus of the heat exchanger for heating unprepared water and heat exchanger tube space of which is connected to the outlet of the synthesis reactor. The heat exchanger at the outlet of the synthesis reactor through the separators are connected by one line to the input of a distillation column for separation of methanol and another line from the supply line converted gas to the synthesis reactor. Cube distillation column is connected with the annular space of the heat exchanger through pipe space which is the line of feed converted gas to the synthesis reactor after the heat exchanger for heating unprepared water.

Implemented by well-known [2] the method of producing methanol includes heating source natural gas from the produced water superheated steam and mixing it with a source of natural gas, single-stage conversion of the gas mixture in the furnace reformer in the converted gas, cooling the converted gas and one-step catalytic conversion to vertirosan gas to the methanol synthesis reactor, the heat of the flue gases of the reformer furnace is used for heating the source of natural gas and produced water, overheated water vapor and gas mixture, and heating the converted gas before entering the synthesis reactor. Heat converted gas is used for heating unprepared water, to obtain from the produced water vapor. Part of the reaction gas leaving the synthesis reactor, into methanol in a distillation column, and the other part as circulating gas is mixed with the converted gas before entering the synthesis reactor. The heat of the reaction gases emerging from the synthesis reactor is used to heat the mixture and converted circulating gas. Heat the converted gas is also used for heating photometering solution to the cube of the distillation column. Regulate the temperature in the synthesis reactor by removal of the cold mixture and converted circulating gas and feed it directly into the reaction zone.

A known method of producing methanol and technological scheme of production of methanol [2] can be used as sources of thermal energy, heat flow resulting from the reaction processes and without additional heat sources. To minimize capital costs was adopted is as technological scheme [2], including one-step conversion of gas-vapor mixture in the reaction tubes of the reformer furnace using Nickel-containing catalyst NIAP-03-01 or Katalko JM 57-4Q and subsequent one-step synthesis of methanol using copper-containing catalyst SNM-1 or Katalko JM 51-8. To simplify the technological process of methanol synthesis temperature control in the reactor for methanol synthesis is carried out automatically by the cold converted gas via the bypass line directly to the reaction zone. In connection with the integration of production units of methanol in the gas field objects adopted technological scheme using as a raw material natural gas Cenomanian deposits without additional preparation.

The technical result of the invention is to provide a joint production of methanol and synthetic liquid hydrocarbons in a process diagram in the process of field training.

The technical result is achieved in that in a method of producing synthetic liquid hydrocarbons (SIU) and methanol from natural gas, comprising heating source natural gas from the produced water superheated steam and mixing it with a source of natural gas, single-stage conversion of the gas mixture in the furnace reformer in the converted gas, cooling the s converted gas one-step catalytic conversion of the converted gas to methanol and the allocation of methanol from the reaction gases, according to the invention a portion of the cooled reformed gas is subjected to catalytic synthesis, the reaction mixture is separated to obtain liquefied petroleum gas (LPG), which is directed to the conversion with the original natural gas and liquid hydrocarbons, and subjected to the stabilization of the obtained synthetic liquid hydrocarbons.

The achievement of the technical result also contributes to the following.

The heat of the flue gases of the reformer furnace is used for heating the source of natural gas and produced water, overheated water vapor and gas mixture.

Heat converted gas is used for heating the circulating liquid hydrocarbons on the stage of stabilization and for heating the circulating methanol at a stage of its selection.

The heat of the reaction gases used for heating the converted gas before the catalytic transformation.

Regulate the temperature of the catalytic conversion by removal of cold converted gas and feed it directly into the reaction zone.

The water is heated by using the heat produced at the stage of catalytic synthesis.

Regulate t is mperature catalytic synthesis by removal of cold converted gas and feed it directly into the reaction zone.

The technical result is also achieved in a device for producing synthetic liquid hydrocarbons (SIU) and methanol containing a supply line for natural gas, sequentially installed and connected system piping heat exchangers for heating natural gas and gas-vapor mixture, the furnace reformer to obtain a converted gas boiler to produce steam and the heat exchanger to superheat, the first separator, the first heat exchanger for heating the converted gas, a synthesis reactor for catalytic production of methanol from the converted gas, the second separator and the column rectification of methanol, and the heat exchanger for heating the produced water, according to the invention the output of the first separator connected also through the second heat exchanger for heating the converted gas from the inlet of the reactor for the synthesis of liquid hydrocarbons, the output of which is serially connected through the first and second cooling heat exchangers with the third and fourth separators, output SIU the third separator is connected to the plate supply of the distillation column stabilization SIU, the exit gas of the fourth separator through the compressor is connected with the line connecting the supply line of the converted gas from the first separator to the synthesis reactor, SIU, and the output for LPG fourth is eparatory connected to the supply line for natural gas.

The achievement of the technical result also contributes to the following.

The output of the reformer furnace in the flue gas is connected with the annular space heat exchangers for heating natural gas, produced water, to superheat steam and heating steam-gas mixture, and a heat exchanger for heating the converted gas.

The output of the reformer furnace in the converted gas is connected to the drain line of the converted gas, sequentially passing through the boiler, the heat exchanger in the line of recycling VAT residue of the distillation column stabilization LPG and heat exchanger on-line recycling of the cubic remainder of the rectification column methanol.

Supply line converted gas before the heat exchanger at the entrance to the methanol synthesis reactor is connected with the latter in the reaction zone.

Cube methanol synthesis reactor is connected to the first separator through the heat exchanger at the inlet to the specified reactor and through the third cooling coils.

Supply line converted gas before the heat exchanger to the inlet of the reactor for the synthesis of SGU connected with the latter in the reaction zone.

The output of the second separator for gas connected to the supply line of the converted gas to the methanol synthesis reactor.

The output of the rectifying column stabilization SIU for distillate is connected via a fourth of lagausie the reflux heat exchanger and the tank top plate of the specified column and line feed natural gas.

The invention is illustrated in the drawing, which shows a diagram of the proposed facility. In the drawing, the threads: I - drained natural gas, II - synthetic liquid hydrocarbons, III - product methanol, IV - stavki in the fuel chain, V - salt-containing effluent VI-flue gases, VII - purified water.

Device for producing synthetic liquid hydrocarbons (SIU) and methanol contains unit 2 heat exchangers, inclusive and connected system piping heat exchangers for heating natural gas and gas-vapor mixture, a heat exchanger for superheated steam and the heat exchanger for heating the produced water. Line 24 of the flow of natural gas through the unit 2 heat exchanger is connected to the input of the reforming furnace 1 to get the converted gas, the output of which is connected to the line 25 of the exhaust reformed gas, which has been consistently found to boiler 4, the heat exchanger 5 on the line of recycling VAT residue of the distillation column 21 of the stabilizing gas and the heat exchanger 6 on the line of recycling VAT residue column 14 of the distillation of methanol, cooling the heat exchanger 7 and the first separator 8.

The output of the reforming furnace 1 on the flue gas is connected with the annular space of the heat exchanger block 2.

After the separator 8 line 25 of the exhaust reformed gas is divided into two: line 26 productoverview gas to the reactor 11 synthesis of methanol and line 27 to supply the converted gas to the reactor 15 synthesis of synthetic liquid hydrocarbons. On line 26 installed compressors 9 and the heat exchanger 10. Line 26 supply the converted gas before the heat exchanger 10 is connected to the reactor 11 in the reaction zone.

Cube reactor 11 synthesis of methanol is connected with the second separator 13 through the heat exchanger 10 through the cooling heat exchanger 12. The output of the second separator 13 for gas connected to the line 26 to supply the converted gas into the reactor 11 synthesis of methanol. The output of the separator 13 for liquid connected to the plate supply of the column 14 of the distillation of methanol.

The output of the first separator 8 is connected through the second heat exchanger 28 to heat the converted gas from the reactor inlet 15 synthesis of liquid hydrocarbons, the output of which is serially connected through the first and second cooling heat exchangers 16 and 18 with the third and fourth separators 17 and 19. Output SIU third separator 17 is connected to the plate supply of the distillation column 21 stabilization SIU. The exit gas of the fourth separator 19 through the compressor 20 is connected with the line connecting line 27 supply the converted gas to the reactor 15 synthesis of SGU, and the output for LPG fourth separator 19 is connected to the line 24 natural gas.

Line 27 of the feed converted gas before the heat exchanger 28 is connected to the reactor 15 synthesis of SGU in the reaction zone. The output of the rectifying column 21 stabilizaciaja for distillate is connected through the fourth cooling heat exchanger 23 and the reflux tank 22 with the upper plate of the specified column 21 and line 24 natural gas.

The proposed method includes steam conversion of natural gas with water vapor, separating the produced synthesis gas into two streams: the first stream is delivered to the methanol synthesis; the second stream is delivered to the synthesis of synthetic liquid hydrocarbons, which are then sent to a hydrocracking unit to unit.

The proposed method of producing synthetic liquid hydrocarbons (SIU) and methanol from natural gas is as follows.

Dry natural gas is regulated by sulphur and Halogens from the preparation unit of natural gas is mixed with the liquefied hydrocarbon gases with columns 21 stabilization SIU and liquefied hydrocarbon gases with objects field treatment of oil or gas condensate (not shown) enters the unit for production of synthesis gas.

Part of the gas intended for the conversion process, enters the third section of the heater natural gas unit 2 heat exchangers, where it is heated to a temperature of 350-450C. Then the natural gas is mixed with superheated steam.

Purified water, brought to the appropriate quality in the primary unit of water, is heated by the heat of reaction for the synthesis of liquid hydrocarbons in the reactor 15 and Pade is camping in the fourth section of the heater unit 2 heat exchangers, where due to the heat of the flue gas is heated to the saturation temperature with partial formation of wet steam. Next, the purified water is fed into the drum separator 3.

Overheated water vapor is carried out in the second section of unit 2 heat exchangers. Technological scheme provides automatic adjustment of the ratio of costs of natural gas and steam entering the methane conversion, maintaining the required ratio of steam: gas=2,73,2:1.

The obtained gas-vapor mixture with a temperature of 350-450C is fed to the heating in the first section of unit 2 heat exchangers. Heated due to the heat of the flue gases to 500-580C vapour-gas mixture is supplied into the reaction tube furnace 1 reforming, where the Nickel catalyst at a temperature of 780-850C and a pressure of 2.0-2.5 MPa reaction takes place the conversion of natural gas with steam with the formation of the converted gas.

The output temperature of the reformed gas, and the temperature of the flue gases at the outlet of the radiant zone of the furnace 1 is automatically controlled by the fuel gas in the bottom of the burner tube furnace 1.

As the fuel gas is part of the natural gas flowing to install. Before feeding into the furnace fuel gas is distributed streams which flow to the pilot and main burners.

Flue gases with temperature is up to 200C after unit 2 heat exchanger by the exhaust fan vented to the atmosphere to a height, providing a dispersion of harmful emissions to the maximum permissible values.

Technological scheme provides the use in the HRSG 4 heat converted gas leaving the reaction zone of the furnace 1 reforming. By cooling the gas with 780-850C to 300-380C produces saturated water vapor pressure of 2.0-2.5 MPa, which from the drum separator 3 is connected to the waste heat boiler 4, is fed to the superheater unit 2 heat exchangers.

In the starting period, if there is insufficient heat of flue gases to preheat the source of natural gas and steam in front of the furnace 1 reforming is provided by the use of additional burners located in the unit 2 heat exchangers.

Heat the converted gas is consistently used in the reboiler of the column 21 stabilization of LPG in the reboiler of the column 14 of the distillation of methanol. After cooling in the heat exchanger 7 converted gas enters the separator 8, where it is separated unreacted water, which is returned to the drum separator 3.

Drained into the separator 8 of the converted gas is divided into two streams: the first stream is delivered to the methanol synthesis, the second stream is directed to the installation of the synthesis of liquid hydrocarbons. If necessary to control the composition of the synthesis gas pot is Kam perhaps the use of a membrane unit for separating a synthesis gas streams. In this case, the first flow mainly contains carbon dioxide, and a second stream enriched in carbon monoxide.

The first stream is mixed with the circulating gas is compressed by the compressor 9 to 5.0 MPa, enters the heat exchanger the heat exchanger 10, where it is heated by the products of the reaction of methanol synthesis. The mixture is converted circulating gas enters the reactor 11 for methanol synthesis.

On the shelves of the reactor 11 is low-temperature copper-containing catalyst, which defines the parameters of the synthesis process: a relatively low temperature of 200280C and low pressure of about 4.5 to 5.5 MPa. To achieve a more complete degree of conversion of methanol provides for circulation of the synthesis gas with a constant output from the separator 13 and the purge gas in the total fuel system to maintain a specified level "innertop". Part of the circulating gas after the separator 13 is directed to mixing with fresh converted gas.

Temperature control in the area of catalysis reactor 11 methanol synthesis is carried out automatically by the cold mixture and converted circulating gas via the bypass lines. The flow of cold gas is collected from the discharge of compressor unit 9.

Cooled in the heat exchangers 10 and 12, the reaction mixture enters the separator 13 to the Department the Department of the crude methanol from the gas-liquid mixture.

Separated in the separator 13 methanol raw is fed to the rectification. The process of distillation of crude methanol is carried out in the column 14.

Heat input to the column 14 is carried by the waste heat recovery converted gas boiler - heat exchanger 6.

The temperature in the bottom part of column 14 is regulated by the bypass converted gas by the heater 6 (not shown). CBM product columns (salt-containing effluents), is sent for recycling.

The distillate of the column (trademark of methanol) is condensed and sent to the warehouse.

The second stream mixes with the circulating gas enters the heat exchanger the heat exchanger 28, where it is heated to the reaction products of the synthesis of liquid hydrocarbons. The mixture is converted circulating gas enters the reactor 15 synthesis of liquid hydrocarbons.

On the shelves of the reactor 15 is an iron or cobalt catalyst, which defines the parameters of the synthesis process. Temperature control in the area of catalysis reactor 15 synthesis is carried out automatically by the cold mixture and converted circulating gas via the bypass lines. The flow of cold gas is collected from the discharge of compressor Assembly 20.

In addition, the temperature control on the shelves of the reactor 15 for accounts is embedded into the reaction zone of the heat exchange structures, the heat which is carried out by heating the source of water produced.

The reaction mixture from the reactor 15 successively cooled in heat exchangers 16 and 18, into the separator 17, where it is separated mixture of synthetic liquid hydrocarbons, hereinafter directed to stabilization in the distillation column 21. The gas phase from separator 17 is cooled in heat exchanger 18 and into the separator 19.

In the separator 19 are separated liquefied hydrocarbon gases that are directed into a stream of dry natural gas that is sent as raw material in the reforming furnace 1.

The gas phase from the separator 19 with regard to maintain a given level inertol" in the circulation system, partly given the overall fuel chain. The residual quantity of the gas phase separator 19 (circulating gas) is further squeezed in the compressor 20, is mixed with fresh converted gas to the reactor 15 synthesis of liquid hydrocarbons.

A mixture of synthetic liquid hydrocarbons from separator 17 is supplied to the plate supply of the distillation column 21. In the column 21 is the branch liquefied petroleum gas (propane-butane) from the stable part of the synthetic liquid hydrocarbons. Heat input to the column 21 is carried out by circulating the cubic product through the heater 5.

The distillate to the Onna 21 (liquefied petroleum gas) is cooled in heat exchanger 23, enters the reflux tank 22 from which is fed to the top tray of the column 21 as irrigation, the carrying amount of the distillate is discharged in a stream of dry natural gas that is sent as raw material in the reforming furnace 1.

CBM product of the column 21, which represents a synthetic liquid hydrocarbons (fraction5+) is sent either in the commodity oil (SGC), or for further processing with the aim of producing motor fuels.

Using the proposed group of inventions through the use of schemes of joint production of methanol and synthetic liquid hydrocarbons under conditions of oil and gas condensate field, has managed to significantly reduce the capital cost per unit of products.

In addition, using the proposed method and the device was able to achieve the following results.

1. Through the use of digester gas steam reforming of hydrocarbons with a Nickel catalyst converted gas does not require additional preparation in the membrane or absorption unit to obtain the optimal ratio of H2:CO:CO2to achieve maximum yield synthetic liquid hydrocarbons.

2. Due to the use for the synthesis of methanol and liquid hydrocarbons reactors shelf type with a chance to view the th sambursky catalyst replacement catalyst may be carried out by facility personnel in the field.

3. Through the use of schema circulating gases in the synthesis of methanol and liquid hydrocarbons were able to significantly increase the yield of the target products.

4. Due to the use as a coolant in the columns stabilization of synthetic liquid hydrocarbons and rectification of crude methanol reformed gas heat reduced consumption of fuel gas.

5. Due to the use as a fuel gas blow-offs with the contours of the circulating gases could reduce the amount of consumed fuel needs of dry natural gas.

6. Due to the use as a component of raw material kiln reforming of liquefied hydrocarbon gases solved the problem of utilization of liquefied petroleum gases, in the absence of the possibility of their transportation.

1. The method of production of synthetic liquid hydrocarbons (SIU) and methanol from natural gas, comprising heating source natural gas from the produced water superheated steam and mixing it with a source of natural gas, single-stage conversion of the gas mixture in the furnace reformer in the converted gas, cooling the converted gas, single-stage catalytic conversion of the converted gas to methanol and the allocation of methanol from the reaction gases, characterized in that the part of ohlord the frame of the converted gas is subjected to catalytic synthesis, the reaction mixture is separated to obtain liquefied petroleum gas (LPG), which is directed to the conversion with the original natural gas and liquid hydrocarbons, and subjected to the stabilization of the obtained synthetic liquid hydrocarbons.

2. The method according to claim 1, characterized in that the heat of the flue gases of the reformer furnace is used for heating the source of natural gas and produced water, excessive heat, water vapor and gas mixture.

3. The method according to claim 1, characterized in that the heat converted gas is used for heating the circulating liquid hydrocarbons on the stage of stabilization and for heating the circulating methanol at a stage of its selection.

4. The method according to claim 1, characterized in that the heat of the reaction gases used for heating the converted gas before the catalytic transformation.

5. The method according to claim 1, characterized in that the temperature is regulated catalytic conversion by removal of cold converted gas and feed it directly into the reaction zone.

6. The method according to claim 1, characterized in that the water is heated by using the heat produced at the stage of catalytic synthesis.

7. The method according to claim 1, wherein regulating the temperature of the catalytic synthesis by removal of cold converted the Aza and feed it directly into the reaction zone.

8. Device for producing synthetic liquid hydrocarbons (SIU) and methanol containing a supply line for natural gas, sequentially installed and connected system piping heat exchangers for heating natural gas and gas-vapor mixture, the furnace reformer to obtain a converted gas boiler to produce steam and the heat exchanger to superheat, the first separator, the first heat exchanger for heating the converted gas, a synthesis reactor for catalytic production of methanol from the converted gas, the second separator and the column rectification of methanol, and the heat exchanger for heating the produced water, characterized in that the output of the first separator is connected through the second a heat exchanger for heating the converted gas from the inlet of the reactor for the synthesis of liquid hydrocarbons, the output of which is serially connected through the first and second cooling heat exchangers with the third and fourth separators, output SIU the third separator is connected to the plate supply of the distillation column stabilization SIU, the exit gas of the fourth separator through the compressor is connected with the line connecting the supply line of the converted gas from the first separator to the synthesis reactor, SIU, and the output for LPG fourth separator is connected to the line podicipedidae gas.

9. Installation according to claim 8, characterized in that the output of the reformer furnace in the flue gas is connected with the annular space heat exchangers for heating natural gas, produced water, to superheat steam and heating steam-gas mixture, and a heat exchanger for heating the converted gas.

10. Installation according to claim 8, characterized in that the output of the reformer furnace in the converted gas is connected to the drain line of the converted gas, sequentially passing through the boiler, the heat exchanger in the line of recycling VAT residue of the distillation column stabilization LPG and heat exchanger on-line recycling of the cubic remainder of the rectification column methanol.

11. Installation according to claim 8, characterized in that the supply line converted gas before the heat exchanger at the entrance to the methanol synthesis reactor is connected with the latter in the reaction zone.

12. Installation according to claim 8, characterized in that the cube of the methanol synthesis reactor is connected to the first separator through the heat exchanger at the inlet to the specified reactor and through the third cooling coils.

13. Installation according to claim 8, characterized in that the supply line converted gas before the heat exchanger to the inlet of the reactor for the synthesis of SGU connected with the latter in the reaction zone.

14. Installation according to claim 8, characterized in that the outlet of the second separator for gas with which dine with the supply line of the converted gas to the methanol synthesis reactor.

15. Installation according to claim 8, characterized in that the output of the rectifying column stabilization SIU for distillate is connected through the fourth cooling heat exchanger and the reflux vessel with the upper plate of the specified column and line feed natural gas.



 

Same patents:

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a method and a plant for methanol production from gas of gas deposits and gas-condensate deposits through synthesis gas using excess heat of the main process of methanol recovery from water-methanol solution returned after inhibition of hydrate formation in a system of collection, treatment and further transport of gas of a complex gas treatment plant (CGTP). Method involves catalytic steam reforming process of gas, heat recovery of converted and flue gases, separation, drying, compression of synthesis gas, synthesis of methanol from synthesis gas on low-temperature catalyst, separation of crude methanol and rectification of methanol, and in addition, stages of methanol recovery from water-methanol solution used in the complex gas treatment plant as a hydrate formation inhibitor and mixing of methanol-rectificate with recovered methanol. In addition, the plant includes a methanol recovery unit and a mixing assembly of synthesised methanol-rectificate and recovered methanol.

EFFECT: creation of an efficient method combining production and recovery of methanol within the framework of a single complex plant; improvement of economic indices of the methanol plant; improvement of quality and reduction of prime cost of methanol production, and elimination of additional environmental gas production risks.

24 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for direct conversion of lower C1-C4 paraffins to oxygenates such as alcohols and aldehydes, which are valuable intermediate products of organic synthesis and can be used as components of engine fuel and/or starting material for producing synthetic gasoline and other engine fuels. The method involves passing a mixture consisting of a lower paraffin or oxygen, diluted with an inert gas or air or pure oxygen, through a catalyst bed at temperature not higher than 350C. The catalyst used is a catalyst system for heterogeneous reactions, which contains microfibre of a high-silica support and at least one active element, the active element being in form of either a MeOxHalv composite or a EwMezOxHaly composite, wherein the element Me in both composites is selected from a group which includes transition metals of groups 5-12 and periods 4 and 5, or elements of lanthanum or lanthanide groups or, preferably, ruthenium; element Hal is one of the halogens: fluorine, chlorine, bromine, iodine, but preferably chlorine; element E in the EwMezOxHaly composite is selected from a group which includes alkali, alkali-earth elements, or hydrogen, and indices w, z, x and y are weight fractions of elements in given composites and can vary in the following ranges: z - from 0.12 to 0.80, x - from 0.013 to 0.34, y - from 0.14 to 0.74, w - from 0 to 0.50.

EFFECT: method enables to achieve high degree of conversion of starting reactants and high selectivity of formation of alcohols.

4 cl, 15 ex

FIELD: chemistry.

SUBSTANCE: present invention relates to a method of producing methanol by bringing a feed stream rich in hydrogen and carbon monoxide in a reactor into contact with a methanol synthesis catalyst to obtain a process stream, followed by cooling thereof, condensation and separation into a gas phase and a liquid phase with crude methanol. The feed stream used is cleaned gas which is obtained by direct-flow gasification of wood processing wastes. The feed stream is enriched with hydrogen by controlled electrolysis of recycled water before bringing the feed stream into contact with a catalyst containing the following, wt %: copper oxide 62, zinc oxide 31, aluminium oxide 7. The feed stream is compressed to pressure of 4.5-5 MPa and then divided into two streams. One stream is fed into the reactor onto the catalyst for contacting through a heat exchanger which simultaneously cools the process stream. The other stream is fed directed onto the catalyst for contacting and reaction temperature is maintained at 250-270C. After final cooling of the process stream in the still residue of the distillation apparatus, it is separated by throttling into a gas phase and a liquid phase. After separation, the gas phase is divided into two streams. One stream is fed for oxidation into a direct-flow gasifier and the other is mixed with the feed stream before compression.

EFFECT: invention enables to obtain the desired product via a wasteless method using one readily available catalyst.

1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to production of natural gas and gas condensate treatment in the field. Proposed method comprises WMS degassing, separating free condensate from WMS, heating WMS in regenerator, methanol recovery from WMS in rectifier, cooling methanol vapors, their condensation and draining into reflux collection tank, feeding collected methanol into tower for refluxing and discharging excess methanol into storehouse. Note here that at all gas fields of the deposit, apart from one, WMS is pre-distilled to increase methanol concentration to level sufficient for its safe transfer via pipelines without freezing and transferred to head WMS high recovery installation to produce commercial methanol for reuse. WMS high recovery installation is located at one of gas fields selected with due allowance for WMS transport logistics.

EFFECT: higher quality and lower costs, increased yield, decreased harmful environmental effects.

2 cl, 1 dwg

FIELD: explosives.

SUBSTANCE: invention relates to the method for production of methanol from synthesis gas, including a stage of synthesis gas compression, a stage of catalytic conversion of synthesis gas into methanol in a reactor unit, comprising several catalytic reactors, including operations of heating and conversion of synthesis gas into methanol in each reactor, an operation of reaction products cooling and methanol release after each reactor, an operation of end gases recycling. Besides, the process is carried out under various pressures and with catalysts loaded into reactors with alternating activity under axial and/or radial direction of reagent flow in catalytic reactors in the temperature range of 160-290C, pressure range of 3-15 MPa, volume speeds of flow 500-10000 hr-1.

EFFECT: method makes it possible to increase efficiency of the process and to produce raw methanol of high quality.

5 cl, 2 ex, 2 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to an oil medium which is suitable for producing dimethyl ether and/or methanol which is used in a synthesis reaction with a suspended layer as a medium which contains a basic component in form of a branched saturated aliphatic hydrocarbon containing 16-50 carbon atoms, 1-7 tertiary carbon atoms, 0 quaternary carbon atoms and 1-16 carbon atoms in branched chains bonded with tertiary carbon atoms; wherein at least one tertiary carbon atom is bonded with hydrocarbon chains with length of 4 or more carbon atoms, lying in three directions. The invention also relates to a method of producing dimethyl ether and a mixture of dimethyl ether and methanol using said oil medium.

EFFECT: use of the present oil medium ensures high efficiency of synthesis.

9 cl, 4 ex, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method for thermal oxidation of methane to methanol, involving heating a portion of the initial methane-containing gas from a complex gas treatment plant in a furnace at given pressure and concentration of oxygen in the initial gas of 20-25 vol. %, fed into a reactor into the space behind the jacket of the tubular cooling zone, and from there into the reaction zone where gas-phase oxidation of methane takes place, with subsequent cooling of the reaction mixture in the tubular cooling zone of the reactor, final cooling of the reaction mixture in a cooler-condenser, during which the cooled reaction mixture is divided into waste gases and liquid products to obtain high- and low-pressure vapour and heating water, wherein regulation of the temperature conditions of the reactor is carried out by feeding into the reaction zone of the reactor a portion of the cold initial gas and measuring heating temperature of a portion of the initial gas fed to the input of the tubular part of the cooling zone of the reactor. Air contained in the initial gas is enriched with oxygen to concentration 25-50 vol. %, and the ratio is equal to -(5-15), where is the bulk concentration of methane in the initial gas; is the bulk concentration of oxygen in the initial gas.

EFFECT: method enables to efficiently obtain the end product in one cycle.

1 ex, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to chemistry. A vapour-phase mixture for producing synthetic gas with molar ratio H2O/C equal to at least 2, which contains water vapour and at least one hydrocarbon or an oxygen-containing hydrocarbon with boiling point ranging from -50 to 370C at atmospheric pressure, is obtained by feeding water vapour into the bottom part of a distillation column and the hydrocarbon or oxygen-containing hydrocarbon into the top part of said distillation column.

EFFECT: invention enables to reduce the content of carbon on the catalyst when producing synthetic gas from said vapour-phase mixture.

3 cl

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing methanol from natural gas, involving heating starting natural gas, obtaining superheated steam from prepared water and mixture thereof with the starting natural gas, single-step conversion of the vapour-gas mixture in a reforming furnace into converted gas, cooling the converted gas and single-step catalytic conversion of the converted gas into methanol in a synthesis reactor, wherein the heat of flue gases from the reforming furnace is used to heat the starting natural gas and the prepared water, superheating the steam and vapour-gas mixture, as well as heating the converted gas before inlet into the synthesis reactor. The invention also relates to apparatus for realising the described method.

EFFECT: use of the present invention increases efficiency of recycling energy from heat flux while simultaneously simplifying the conversion and synthesis processes.

11 cl, 1 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: Invention relates to methanol production plant and to method of methanol production by oxidising methane-containing gas at said plant. Proposed plant comprises plant for integrated gas treatment, reactor gas-phase methane-containing gas oxidation consisting of gas-to-gas heat exchanger of reaction zone and gas-to-water heat exchanger of cooling zone, refrigerator-condenser, rectification unit, ecological system and gas burner. Note here that reaction mix maximum heat zone accommodates extra reactor made up of cylindrical tube with feeder of extra portion of cold methane-containing gas including natural gas, refrigerator-condenser communicated via injector with one of gas burner inlets.

EFFECT: higher yield of methanol per 1 m3 of methane in single cycle.

1 ex, 1 dwg

FIELD: process engineering.

SUBSTANCE: invention relates to production of synthesis gas. Proposed method comprises the steps that follow. Hydrocarbon reforming in the presence of steam and one and more catalysts in the first reaction zone to obtain exit flow containing part of hydrocarbon, carbon monoxide, carbon dioxide and hydrogen at first temperature. Note here that said first reaction zone can included one or more tubes with catalyst. In includes indirect heating of exit flow from first temperature to second temperature. Reforming of exit flow is performed at second temperature in the presence of one or more oxidisers and one or more second catalysts under conditions sufficient for production of synthesis gas with temperature of about 1030C or higher. Said flow contains hydrogen, carbon monoxide, carbon dioxide and less than about 5 mol % of methane per dry substance. Note here that synthesis gas is used for indirect heating of exit flow from first temperature to second temperature.

EFFECT: power savings.

21 cl, 1 tbl, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to catalysts. Described is a catalyst for use in a high-temperature shift reaction, which, in its active form, contains a mixture of a zinc-aluminium spinel and zinc oxide combined with an alkali metal selected from a group comprising Na, K, Rb, Cs and mixtures thereof, said catalyst having molar ratio Zn/Al ranging from 0.5 to 1.0, and alkali metal content ranging from 0.4 to 8.0 wt % with respect to the weight of the oxidised catalyst. Described is a method of enriching a synthesis gas mixture with hydrogen or carbon monoxide by reacting said synthesis gas mixture with the catalyst described above.

EFFECT: high catalyst activity.

8 cl, 8 tbl, 31 ex

FIELD: chemistry.

SUBSTANCE: invention relates to field of chemistry. To obtain hydrogen reaction of steam catalytic conversion of carbon-containing liquid is carried out with obtaining hydrogen-containing reaction products. Reaction products are directed on output of cathode space for electrolysis in high temperature electrolyser, on outlet from cathode space reaction flow, which contains synthesis-gas, directed on catalytic synthesis of carbon-containing liquid, is separated. Oxygen is released in anode space, separated from cathode space by electrolytic layer. Carbon-containing liquid is returned to the start of process for conversion, and hydrogen, obtained in process of carbon-containing liquid synthesis, is purified from carbon oxides.

EFFECT: hydrogen obtaining.

11 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to production of catalysts for thermochemical conversion hydrocarbon and oxygen-containing fuels through heat of exhaust gases of internal combustion engines, which are a component part of hybrid power installations. Described is a catalyst for thermal recuperation of heat of exhaust gases of an internal combustion engine, having an active component deposited on a support which is a heat-conducting structured material located on flat panels consisting of exothermic and endothermic channels and consists of alternating flat and corrugated heat-conducting porous metal catalyst bands which form channels for passage of the reacting mixture.

EFFECT: high utilisation of heat in hybrid power installations.

3 cl, 3 ex, 3 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to chemistry. Apparatus for producing hydrogen from water consists of a housing in which there is a reactor, where electrodes are mounted while applying voltage across said electrodes, the apparatus being characterised by that working electrodes are in form of mesh cylinders made from aluminium alloys, inserted into each other with a spacing to form a bundle, wherein an atomiser is inserted from the bottom of the bundle, the atomiser being connected to a high pressure pump which is connected to a heating vessel mounted at the exhaust manifold of a car, which along with the bundle is connected to a source of intermitted high voltage, and the bundle of mesh cylinder electrodes is mounted in a high-voltage acceleration electric field between electrodes connected to a source of a high-voltage field.

EFFECT: low cost of producing hydrogen and high efficiency.

FIELD: chemistry.

SUBSTANCE: invention relates to a method of producing hydrocarbons, hydrogen and oxygen using carbon dioxide and water. According to the method, water is saturated with carbon dioxide to obtain carbonated water; the carbonated water is passed through at least one reactor having a catalyst to conduct the reaction: nCO2+[4n+2(k+1)]H2O=CnH2n+2+[3n+2k+1]H2+[3n+k+1]O2, where k is an integer greater than or equal to 0, n is an integer greater than or equal to 1, to obtain hydrocarbons, hydrogen and oxygen, further fed into at least one separator; reaction products from the source carbonated water are separated in at least one separator by separating the gas phase and the liquid phase, wherein hydrocarbons are separated from the liquid phase and the gas phase, and hydrogen and oxygen are further separated from the gas phase.

EFFECT: method enables to simultaneously obtain hydrocarbons, hydrogen and oxygen while reducing power consumption while reducing environmentally hazardous products.

10 cl, 1 ex, 5 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to field of chemistry. Synthesis-gas from gas-generator 10 is supplied into reactor 64 for conversion of carbon oxide into carbon dioxide. From reactor 64 synthesis-gas is directed into absorption unit 12, containing one or several membrane contact filters 72. Synthesis-gas can be kept in internal volume 74, and in internal volume 76 - solvent. Membrane contact filters are located between two volumes 74 and 76. Ennobled synthesis-gas, leaving unit 12, consisting mainly of hydrogen, is supplied into gas turbine 6. Output gas from gas turbine 6 is supplied into system 8, where gas is caught and used for steam production. Steam, obtained in system 8, is supplied into system 66 for reduction of solvent.

EFFECT: inventions make it possible to reduce production expenditures due to reduction of equipment size and quantity of solvent.

10 cl, 4 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to method of obtaining synthesis-gas. Method includes stages, in which: vapour-phase mixture, consisting of water vapour and dispersed hydrocarbon or oxidised hydrocarbon, is prepared, and catalytic conversion of vapour-phase mixture into synthesis-gas is performed in installation for reforming. Vapour-phase mixture is prepared by dispersion of hydrocarbon or oxidised hydrocarbon through atomiser in such a way that hydrocarbon or oxidised hydrocarbon is present in form of drops with drop size smaller than 500 mcm, and time to achievement of its complete evaporation does not exceed 0.5 seconds, and hydrocarbon or oxidised hydrocarbon has temperature of boiling at atmospheric pressure in the range from -50 to 370C, and vapour phase has molar ratio H2O/C, at least, 2. Drop-generating atomiser is dispersive atomiser, into which water vapour is supplied. Hydrocarbon or oxidised hydrocarbon is at temperature below 180C and is supplied into atomiser through vapour chambers, followed by heating device.

EFFECT: invention ensures alternative and economically profitable synthesis-gas manufacturing.

12 cl

FIELD: chemistry.

SUBSTANCE: invention relates to catalysts of hydrogen burning. Described is catalyst of hydrogen burning, which includes catalytically active metal, applied on catalyst carrier, formed by inorganic oxide, with carrier including organic silane with at least one alkyl group of three or fewer carbon atoms, by substitution of bound to end of each of certain part or to all hydroxyl groups on the surface of carrier; and catalytically active metal is applied on catalyst carrier, including bound to it organic silane. Described is method of obtaining said catalyst and its application in hydrogen burning, in particular, in reactor of catalytic oxidation, located in installation for tritium extraction.

EFFECT: increase of catalyst activity.

7 cl, 2 dwg, 5 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to an apparatus for producing hydrogen. The apparatus has a reaction chamber surrounded by a pipe, in which a mixture of water vapour and carbon-containing material is converted by steam reforming, and a partition wall which is partially, selectively permeable for hydrogen, through which hydrogen formed during steam reforming can be continuously removed from the reaction chamber with high purity and at pressure below the pressure in the reaction chamber and higher than ambient pressure. Portions of the partition wall that are selectively permeable for hydrogen lie such that on the entire surface of such a portion between the reaction chamber and the hydrogen outlet side there is always a drop of partial pressure, wherein the partition wall consists of a plurality of thermodiffusion separating pipes connected to form a unit.

EFFECT: obtaining high-purity hydrogen and low capital costs by excluding separation and/or compression of hydrogen.

2 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention refers to a method and a plant for methanol production from gas of gas deposits and gas-condensate deposits through synthesis gas using excess heat of the main process of methanol recovery from water-methanol solution returned after inhibition of hydrate formation in a system of collection, treatment and further transport of gas of a complex gas treatment plant (CGTP). Method involves catalytic steam reforming process of gas, heat recovery of converted and flue gases, separation, drying, compression of synthesis gas, synthesis of methanol from synthesis gas on low-temperature catalyst, separation of crude methanol and rectification of methanol, and in addition, stages of methanol recovery from water-methanol solution used in the complex gas treatment plant as a hydrate formation inhibitor and mixing of methanol-rectificate with recovered methanol. In addition, the plant includes a methanol recovery unit and a mixing assembly of synthesised methanol-rectificate and recovered methanol.

EFFECT: creation of an efficient method combining production and recovery of methanol within the framework of a single complex plant; improvement of economic indices of the methanol plant; improvement of quality and reduction of prime cost of methanol production, and elimination of additional environmental gas production risks.

24 cl, 1 dwg

Up!