RU2614956C1 - Plant for producing synthetic liquid fuel - Google Patents

Plant for producing synthetic liquid fuel Download PDF

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RU2614956C1
RU2614956C1 RU2016112165A RU2016112165A RU2614956C1 RU 2614956 C1 RU2614956 C1 RU 2614956C1 RU 2016112165 A RU2016112165 A RU 2016112165A RU 2016112165 A RU2016112165 A RU 2016112165A RU 2614956 C1 RU2614956 C1 RU 2614956C1
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unit
input
connected
gas
supply line
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RU2016112165A
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Игорь Павлович Афанасьев
Юрий Владимирович Лебедев
Денис Вячеславович Новиков
Алексей Борисович Юмашев
Анатолий Владимирович Мамаев
Сергей Алексеевич Сиротин
Дмитрий Аркадьевич Мирошниченко
Светлана Владимировна Семёнова
Лариса Васильевна Моргун
Вячеслав Александрович Логинов
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Публичное акционерное общество "Газпром"
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Abstract

FIELD: chemistry.
SUBSTANCE: plant for producing synthetic liquid fuel can be used, in particular, for performing the chemical process of producing synthetic liquid fuel. The plant for producing synthetic liquid fuel, which comprises a unit for the raw material gas adsorptive purification from the sulfur compounds, a unit for converting methane into synthesis gas, a unit for the synthesis gas purification from CO2, a liquid hydrocarbons synthesis unit, a synthetic liquid hydrocarbons (SLH) stabilization unit, a SLH hydro-treating unit, a SLH hydroskimming unit, a synthetic liquid fuels (GTL) fractionation unit, a water recycling unit and a hydrogen circulation unit. The units are interlinked functionally.
EFFECT: simplification of the technological process of producing synthetic liquid fuels due to the organization of self-providing the individual process stages with hydrogen-containing gas, excluding the stage of target synthesis products extraction from exhaust gases, and due to performing the hydro-treating and hydroskimming of the synthetic liquid hydrocarbons without prior fractionation.
1 dwg

Description

The invention relates to the chemical industry and can be used, in particular, for carrying out a chemical process for producing synthetic liquid fuel.

A known installation for producing synthetic liquid fuels (SFA) from coalbed methane. The installation for the production of SZHT includes a supply line for the feed stream of methanol, a line of circulating gas, a drainage line, an outlet line of SZHT, a site for producing model synthesis gas and a site for producing SZHT in the form of a conversion unit for model syngas. A compressor, a heater, synthesis gas catalytic conversion reactors, a condenser-condenser, and a three-phase separator connected to the technological chain form a block for the conversion of model synthesis gas to FGM. A two-phase separator is integrated between the condenser refrigerator and the three-phase separator. The unit for producing model synthesis gas contains a decomposition unit for the feed stream — methanol and a separator. The compressor intake is connected to the gas outlet of the separator of the model syngas production unit. The decomposition unit of the feed stream - methanol is made in the form of an evaporator connected to each other, two reactors for the decomposition of the feed stream - methanol, a condenser refrigerator, a mixer. In the installation, the model syngas conversion unit in the SZT contains two synthesis gas catalytic conversion reactors (Patent RU 61278 U1, IPC C07C 1/04 (2006.01), published on February 27, 2007).

The task to which the claimed technical solution is directed is to create a plant for producing synthetic liquid fuel, which eliminates the stage of extraction of target synthesis products from exhaust gases in particular and simplifies the process of producing synthetic liquid fuels in general.

The technical result, which the claimed invention is directed to, is to simplify the process of producing synthetic liquid fuels by organizing self-sufficiency of individual technological stages with hydrogen-containing gas (purification of raw gas from sulfur compounds, hydrotreating and hydrofining of synthetic liquid hydrocarbons (LSS)), eliminating the target extraction stage synthesis products from the exhaust gases (due to the supply of exhaust gases to the stabilization section of the coolant), as well as through Wastewater treatment and hydrofining without preliminary fractionation.

The specified technical result is achieved by creating a synthetic liquid fuel production unit, which includes a unit for adsorption purification of raw gas from sulfur compounds, a unit for converting methane to synthesis gas, a unit for purifying synthesis gas from CO 2 , a unit for synthesizing liquid hydrocarbons, a stabilization unit synthetic liquid hydrocarbons (LFU), LIU hydrotreating unit, LIU hydrofining unit, synthetic liquid fuel fractionation unit (LFU), water circulation unit and hydrogen circulation unit, the first entrance block adsorption purification of raw gas from sulfur compounds is connected to the supply line of raw natural gas from the factory network, the second input is connected to the supply line of hydrogen-containing gas from the liquid hydrocarbon synthesis unit, the third input is connected to the first supply line of fuel gas from the hydrogen circulation unit, in addition, the block of adsorption purification of raw natural gas has an outlet of purified natural gas associated with the first input of the block for converting methane to synthesis gas, while the block for converting methane into synthesis gas has a second move - input of technical oxygen, a third input connected to the supply line CO 2 from the synthesis gas purification unit of the CO 2, the fourth input connected to the supply line of the superheated steam from the block water circulation, a first input of which is connected to a line supplying the condensed water from the unit conversion methane to synthesis gas, a second input connected with the water circulation unit supplying steam condensate line for regeneration of diethanolamine (DEA) from synthesis gas purification unit of the CO 2, the third input is connected to a line supplying water from the reaction block synthesis of liquid hydrocarbons fourth input connected to the steam supply line from the liquid hydrocarbon synthesis unit, the fifth input is connected to the water condensate supply line from the SLC stabilization unit, and the sixth input is connected to the water condensate supply line from the SLC fractionation unit, the first input of the synthesis gas purification unit from CO 2 is connected to the supply line of synthesis gas containing CO 2 from the methane to synthesis gas conversion unit, and the second input of the synthesis gas cleaning unit from CO 2 is connected to the steam supply line for regenerating the DEA solution from the water circulation unit, the first input of the hydrogen circulation unit is connected to whether the stabilization gas supply from the stabilization unit of the coolant, the second input is connected to the supply line of a mixture of hydrogen and hydrocarbon gases from the hydrofinishing unit of the coolant, the third input is connected to the supply of separation gas from the hydrofining unit of the coolant, the fourth input is connected to the supply of separation gas from the fractionation unit of the coolant , the first input of the liquid hydrocarbon synthesis unit is connected to the supply line of superheated boiler water from the water circulation unit, the second input is connected to the second supply line of fuel gas from the hydrogen circulation unit, and the third input One is connected to the supply line of CO 2 purified from the synthesis gas from the synthesis gas from CO 2 block, the first input of the LNG stabilization unit is connected to the third line of the fuel gas supply from the hydrogen circulation unit, the second input is to the unstable LNG supply line from the synthesis unit liquid hydrocarbons, the third inlet - with the line for supplying exhaust gas from the liquid hydrocarbon synthesis unit, and the fourth inlet - with the line for propane supply, the first inlet of the LHU hydrotreating unit is connected to the line for supplying a stable wide fraction of LIU from the LIU stabilization unit, and the second inlet - with a supply line of circulating hydrogen from the hydrofinishing unit of the LHF, the first input of which is connected to the feed line of a hydrotreated wide fraction of the FFU from the hydrofining unit of the FFU, the second input is connected to the supply line of purified hydrogen from the hydrogen circulation unit, the third input is connected to the fourth supply line of fuel gas from hydrogen circulation unit, and the fourth input is connected to the supply line of the SZHT fraction 360-540 ° C for recycling from the fractionation unit of the SZhT, while the first input of the fractionation unit of the SZhT is connected to the steam supply line from the block and the water circulation, the second inlet with a fifth line of fuel gas supply from the hydrogen circulation unit, and the third inlet with the line of supplying a wide fraction of SZHT from the SZhU hydrofining unit, and the synthesis gas purification unit from CO 2 has an outlet for CO 2 output to the atmosphere, the hydrogen circulation unit has an outlet for supplying excess fuel gas to the factory network, the water circulation unit has an outlet for supplying excess steam from the water circulation unit to the factory network, and the NLW fractionation unit has the NLW fractions output: “start of boiling” - 150 ° C, 150-180 ° C, 180-280 ° C, 280-360 ° C and 360-540 ° C for I further use them as fuel components.

The invention is illustrated in the drawing.

The installation for producing synthetic liquid fuel (SZHT) includes ten main blocks:

- block 1 adsorption gas purification from sulfur compounds;

- unit 2 for the conversion of methane to synthesis gas;

- block 3 purification of synthesis gas from CO 2 ;

- block 4 synthesis of liquid hydrocarbons;

- block 5 stabilization LSS;

- unit 6 hydrotreating SJU;

- block 7 hydrofining SJU;

- block 8 fractionation of SZHT;

- block 9 water circulation;

- block 10 of the circulation of hydrogen.

Block 1 adsorption purification of gas from sulfur compounds includes a furnace, a hydrogenation reactor and adsorbers. Block 2 of the conversion of methane to synthesis gas includes a saturator, recuperative heat exchangers, reactors, air-cooling units, and a separator. The synthesis gas purification unit 3 for CO 2 includes an absorber, stripper, expander, recuperative heat exchangers, air cooling apparatus, a separator and a steam evaporator. Block 4 for the synthesis of liquid hydrocarbons includes a furnace, a synthesis reactor, recuperative heat exchangers, an air cooling apparatus, a separator, a membrane hydrogen evolution unit, and a compressor. Block 5 stabilization SZHU includes a furnace, distillation column, recuperative heat exchangers, a propane refrigerator and a separator. The unit 6 hydrotreating SJU includes a reactor, an air cooling apparatus, a separator and pumps. Block 7 hydrofining SZHU includes a furnace, a reactor, recuperative heat exchangers, air cooling apparatus, separators and pumps. Block 8 fractionation SZHT includes a furnace, distillation column, stripping columns, recuperative heat exchangers, air cooling apparatus, separators and pumps. Block 10 of the circulation of hydrogen contains an air cooling apparatus, a separator, adsorbers, compressors.

Block 1 adsorption purification of raw gas from sulfur has three inputs: the first input is the input 11 of raw natural gas from the factory network, the second input connected to the line 25 for the supply of hydrogen-containing gas from the unit for the synthesis of liquid hydrocarbons, the third input connected to the first line 48 for the supply of fuel gas from the hydrogen circulation unit, also the adsorbent purification unit 1 of the feed gas has an outlet 12 of purified natural gas associated with the first input of the unit 2 for converting methane to synthesis gas. In this case, the unit 2 for converting methane to synthesis gas has three more inputs: the second input is the input of technical oxygen 13, the third input connected to the line 16 for supplying carbon dioxide from the unit 3 for cleaning the synthesis gas from CO 2 , and the fourth input associated with a line 14 for supplying superheated steam from the water circulation unit 9. The water circulation unit 9, in turn, has six inputs: the first input connected to the water condensate supply line 17 from the methane to syngas conversion unit, the second input connected to the steam condensate supply line 19 for diethanolamine (DEA) regeneration from the synthesis purification unit 3 gas supply from CO 2 , the third inlet connected to the line 23 for supplying reaction water from the liquid hydrocarbon synthesis unit 4, the fourth inlet connected to the line 24 for supplying steam from the liquid hydrocarbon synthesis unit 4, the fifth inlet connected to the line 29 for supplying water condensate from block 5 stub ization SZHU, and a sixth input coupled to a line 41 supplying the condensed water from the fractionation unit 8 of synthetic liquid fuels (GTL). The synthesis gas purification unit 3 from CO 2 has two inputs: the first input is connected to the synthesis gas supply line containing CO 2 from the methane to syngas conversion unit 2, and the second input is connected to the steam supply line 18 for regenerating the solution DEA from block 9 of the water cycle. The hydrogen circulation unit 10 has four inputs: the first input connected to the stabilization gas supply line 30 from the SJU stabilization unit 5, the second input connected to the hydrogen and hydrocarbon gas mixture supply line 34 from the SJU hydrotreating unit 7, the third input connected to the line 38 the gas supply of separation from the unit 7 hydrofining SZHU, and the fourth inlet connected to the line 40 of the gas supply of separation from block 8 fractionation SZHT. Block 4 of the synthesis of liquid hydrocarbons has three inputs: the first input connected to the supply line 22 of the superheated boiler water from the water circulation unit 9, the second input connected to the second supply line 49 of the fuel gas from the hydrogen circulation unit 10, and the third input connected to the line 21 supply purified from CO 2 synthesis gas from block 3 for the purification of synthesis gas from CO 2 . The stabilization unit 5 of the SJU has four inputs: the first input connected to the third 50 line of supply of fuel gas from the hydrogen circulation unit 10, the second input connected to the supply line 27 of unstable SJU from the unit 4 for the synthesis of liquid hydrocarbons, the third input connected to the supply line 26 off-gas from liquid hydrocarbon synthesis unit 4, and a fourth inlet connected to propane supply line 28. Block 6 hydrofinishing SZHU has two inputs: the first input connected to the supply line 31 of a stable wide fraction of FFS from the stabilization unit 5 of the FFS, and the second input connected to the supply line 32 of circulating hydrogen from block 7 hydrofining SZHU. The first input of the unit for hydrofining of the SJU is connected to the supply line 33 for hydrotreated a wide fraction of the SJU from the unit 6 for hydrotreating the SJU, the second input to the line 35 for supplying purified hydrogen from the hydrogen circulation unit 10, the third input to the fourth line 51 for supplying fuel gas from the hydrogen circulation unit and the fourth inlet - with a supply line 36 of the SZHT fraction 360-540 ° C for recycling from block 8 of the SZhT fractionation. In this case, the first input of the FAC fractionation unit 8 is connected to the steam supply line 39 from the water circulation unit, the second input - to the fifth fuel gas supply line 52 from the hydrogen circulation unit 10, and the third input - to the supply line of the wide FAC fraction 37 from the FGC unit 7 . The synthesis gas purification unit 3 from CO 2 has a line 20 for discharging CO 2 into the atmosphere, the hydrogen circulation unit 10 has a line 53 for supplying excess fuel gas to the factory network, the water circulation unit has line 47 for supplying excess steam from the water circulation unit to the factory network and the block of fractionation of SZhT has lines 42-46 of an exit of fractions of SZhT: "the beginning of boiling" - 150 ° C, 150-180 ° C, 180-280 ° C, 280-360 ° C and 360-540 ° C for their further use as fuel components.

Installation works as follows.

Raw natural gas through line 11 enters block 1 of adsorption gas purification from sulfur compounds from the factory network with a pressure of not more than 6.0 MPa and a temperature of not more than 40 ° C, is throttled and mixed with hydrogen-containing gas coming through line 25 from synthesis unit 4 SJU. The resulting mixture of hydrogen-containing and natural gas is heated in the furnace to a temperature of 370 ° C due to the heat generated during the combustion of fuel gas, sequentially passes the stage of catalytic hydrogenation of sulfur-containing organic compounds to hydrogen sulfide and its absorption by an adsorbent based on zinc oxide. Fuel gas via line 48 is supplied from the hydrogen circulation unit 10.

Purified natural gas with a sulfur content of not more than 0.5 ppm is sent via line 12 to the unit 2 for converting methane to synthesis gas, where due to the interaction of the hydrocarbon components of natural gas with steam, carbon dioxide and oxygen at temperatures of 850-1100 ° C the reaction of the formation of a mixture of carbon monoxide and hydrogen (synthesis gas). When cooling the resulting mixture, water condensate forms, which is sent via line 17 to the water circulation unit 9.

The technical oxygen required for the synthesis gas production process via line 13 is supplied from an air separation unit (not shown) with an overpressure of not more than 4.0 MPa, the necessary steam is supplied via line 14 from the water circulation unit 9.

The cooled synthesis gas is sent through line 15 to the CO 2 purification unit for synthesis gas synthesis, where absorption cleaning of the synthesis gas from diethanolamine (DEA) from the carbon dioxide contained in it proceeds in the packed column. The regeneration of a saturated DEA solution is carried out in a stripper, a packed column. The heat required for the regeneration of the saturated DEA solution is communicated to the solution in riboilers heated by low pressure dew steam 18, which comes from the water circulation unit 9. Steam condensate along line 19 is sent to the water circulation unit 9.

A part of the carbon dioxide released during desorption from the saturated DEA solution is compressed and sent via line 16 to the unit 2 for converting methane to synthesis gas. Excessive amounts of carbon dioxide through line 20 are discharged into the atmosphere.

The purified synthesis gas is sent through line 21 to the LNG synthesis unit 4, where it is mixed with the circulation gas stream, heated in the furnace due to the heat generated during the combustion of fuel gas supplied via line 49, and passes through three stages of hydrocarbon synthesis on a cobalt-containing synthesis catalyst Fischer-Tropsch at a temperature of 210 ° C-220 ° C and a pressure of 2.0 ÷ 2.5 MPa.

To maintain a constant temperature regime of synthesis reactors, water is supplied to the reactor shirts from the water circulation unit 9 through line 22, overheated to the temperature of the reaction. The resulting steam from the reaction heat of the reaction through line 24 is sent to the water circulation unit 9.

After each step of the synthesis, the obtained gas-liquid mixture is cooled, then it is separated into liquid and gas phases. The gas phases leaving the first and second stages of synthesis are heated in regenerative heat exchangers and sent to the next stage of synthesis. The gas phase emerging from the third stage of synthesis is divided into two streams — circulation gas and exhaust gas.

The off-gas through line 26 is sent to the LNG stabilization unit 5 to extract C5 + hydrocarbons from it, and the circulation gas enters the membrane unit, where a partial evolution of hydrogen-containing gas from the gas stream takes place. Hydrogen-containing gas is sent via line 25 to sulfur adsorption purification unit 1 of natural gas. The flow of circulation gas after the release of hydrogen-containing gas is mixed with purified syngas.

The liquid phase from all three stages of synthesis is divided into unstable synthetic liquid hydrocarbons and reaction water (a by-product of synthesis). The reaction water through line 23 is sent to the water treatment unit 9 of the water circulation, and unstable synthetic liquid hydrocarbons through line 27 to the unit 5 stabilization LF.

The stabilization process is carried out in a plate-type distillation column stabilizer with preliminary regenerative heating of the feed at a pressure of about 1.9-2.0 MPa and a column top temperature of approximately + 43 ° C, bottom + 317 ° C. A propane refrigerator is used to cool the reflux condenser, and a fire furnace is used to heat the column cube.

The fuel gas necessary for the stabilization process via line 50 comes from the hydrogen circulation unit 10, and propane via line 28 from the propane production unit (not shown).

Vapors from the top of the stabilizer are cooled, condensed and separated into gas (stabilization gas), hydrocarbon and water phases (water condensate). A stabilization gas containing hydrogen is sent via line 30 to a hydrogen circulation unit 10. The hydrocarbon phase is fed to the irrigation column of the stabilizer, and water condensate through line 29 is sent for purification in block 9 of the water circulation.

From the lower part of the stabilizer, the balance amount of a stable wide fraction of coolant is removed, which is sent via line 31 to the coolant hydrotreating unit 6.

A stream of a stable wide fraction of LFU is mixed with circulating hydrogen coming through line 32 from the LFU hydrofining unit 7 and is hydrotreated from unsaturated hydrocarbons at a temperature of 150 ° C and a pressure of 1.5 MPa on a hydrotreating catalyst.

The resulting gas product mixture is cooled and separated into a gas (a mixture of hydrogen and hydrocarbon gases) and a liquid phase (hydrotreated a wide fraction of LSS).

A mixture of hydrogen and hydrocarbon gases from block 6 is sent via line 34 to block 10 of hydrogen circulation for mixing with the stabilization gas coming through line 30 and subsequent purification from hydrocarbons, and the hydrotreated broad fraction of coolant through line 33 is sent to block 7 for hydrofining of the coolant.

The hydrotreated broad fraction of LFG is mixed with purified hydrogen coming from line 35 from block 10 of the hydrogen circulation, and then sent to mix with the LWF fraction 360-540 ° C, returning through line 36 as recycle from block 8 of the LFW fractionation.

The resulting mixture of hydrotreated FGF, FFL fractions 360-540 ° C and hydrogen is heated in the furnace to the temperature of the onset of the reaction due to the heat generated during the combustion of fuel gas 51 and is fed to the hydrofining stage, where at a temperature of 350 ° C and a pressure of 5 MPa on the catalyst hydrofining as a result of cracking and isomerization of hydrocarbons structural changes occur in the composition of the mixture.

The gas-liquid mixture after the hydrofining step is cooled, partially condensed, and enters the two-stage separation stage to separate unreacted hydrogen and the separation gas formed as a result of catalytic processes.

Hydrogen released from the unit 7 hydrofining SZHU after depressurizing through line 32 is sent to the unit 6 hydrotreating SZHU. The separation gas through line 38 is supplied to the hydrogen circulation unit 10, to the fuel gas line.

A wide fraction of SZHT on line 37 is fed for separation into narrow fuel fractions in block 8 fractionation of SZHT, where it is heated in a furnace to a temperature of 330 ° C due to the heat generated during the combustion of fuel gas, and under a pressure of 0.8 MPa is sent to the distillation column for separation into fractions SZHT 42-46: NK-150 ° C, 150-180 ° C, 180-280 ° C, 280-360 ° C and 360-540 ° C. Fuel gas via line 52 is supplied from a hydrogen circulation unit 10.

Vapors of the NK-150 ° C fraction (NK - the beginning of boiling) are discharged from the top of the column, cooled, and fed to a three-phase separator, where the gas phase is separated from the liquid, as well as water condensate from liquid hydrocarbons. In this case, the separation gas through line 40 is sent to the hydrogen circulation unit 10, the water condensate through line 41 is sent for purification to the water circulation unit 9, the liquid phase of the hydrocarbons is supplied to the column irrigation, and its excess volumes are removed from the unit in the form of the NK-150 ° SZhT fraction C.

Fractions SZHT 150-180 ° C, 180-280 ° C, 280-360 ° C are selected from the column as side shoulder straps. Fraction SZHT 360-540 ° C from the bottom of the column is fed as recycle through line 36 to block 7 hydrofining SZHU with the possibility of withdrawal of this fraction from the installation.

To improve the stripping of light fractions, sharp water vapor is supplied to the bottom of the column through line 39 from block 9 of the water circulation.

The hydrogen circulation unit 10 performs the functions of organizing a hydrogen recycle and preparing fuel gas for its further use at various stages of production. In this case, hydrogen is purified from impurities on the basis of a short-cycle adsorption unit, which is part of the unit. Excess fuel gas 53 is routed to the factory network.

The water circulation unit is used to collect reaction water and water condensate formed at various stages of production, their purification and preparation for reuse in technological processes, as well as for the production of steam with the necessary parameters. Excess steam 47 is routed to the factory network.

Claims (1)

  1. Installation for producing a synthetic liquid fuel, which was composed of unit adsorption treatment of feed gas from the sulfur compounds, methane conversion unit into a synthesis gas purification unit of the synthesis gas from the CO 2, the block synthesis of liquid hydrocarbons flow stabilizing synthetic liquid hydrocarbons (SZHU) SJU hydrotreating unit, SJU hydrotreating unit, synthetic liquid fuel fractionation unit (SJT), water circulation unit and hydrogen circulation unit, the first input of the adsorption unit for cleaning raw gas from sulfur compounds connected to the feed line of natural gas from the factory network, the second input is connected to the supply line of hydrogen-containing gas from the liquid hydrocarbon synthesis unit, the third input is connected to the first supply line of fuel gas from the hydrogen circulation unit, in addition, the adsorption purification unit of raw natural gas has an output purified natural gas associated with the first input of the unit for converting methane to synthesis gas, while the unit for converting methane to synthesis gas has a second input - the input of technical oxygen, the third input associated with by supplying CO 2 from the synthesis gas purification unit from CO 2 , the fourth input connected to the supply line of superheated steam from the water circulation unit, the first input of which is connected to the supply line of water condensate from the methane to synthesis gas conversion unit, the second input of the water circulation unit is connected with a steam condensate supply line for diethanolamine (DEA) regeneration from the synthesis gas purification unit from CO 2 , a third input is connected to a reaction water supply line from a liquid hydrocarbon synthesis unit, a fourth input is connected to a steam supply line from a liquid hydrocarbon synthesis unit Dov, the fifth input is connected to the supply line of water condensate from the stabilization unit of the SZHU, and the sixth input is connected to the supply line of water condensate from the fractionation unit of the SZHT, the first input of the synthesis gas purification unit from CO 2 is connected to the supply line of synthesis gas containing CO 2 , from the methane to syngas conversion unit, and the second input of the synthesis gas purification unit from CO 2 is connected to the steam supply line for regenerating the DEA solution from the water circulation unit, the first input of the hydrogen circulation unit is connected to the stabilization gas supply line from the stabilization gas unit, second the first input is connected to the supply line of a mixture of hydrogen and hydrocarbon gases from the hydrofluorine unit of the SJU, the third input is connected to the line of supply of the separation gas from the hydrofining unit of the SJU, the fourth input is connected to the supply line of the separation gas from the fractionation unit of the SJF, the first input of the liquid hydrocarbon synthesis unit is connected to the supply line of the superheated boiler water from the water circulation unit, the second input is connected to the second supply line of the fuel gas from the hydrogen circulation unit, and the third input is connected to the supply line of the synthesis gas purified from CO 2 from the unit purification of syngas from CO 2 , the first input of the stabilizing liquid cooling unit is connected to the third line of supplying fuel gas from the hydrogen circulation unit, the second input is connecting to the line of supplying unstable coolants from the liquid hydrocarbon synthesis unit, and the third input is connecting to the line of supplying exhaust gas from the synthesis unit liquid hydrocarbons, and the fourth inlet is with the propane supply line, the first inlet of the SJU hydrotreating unit is connected to the supply line of a stable wide fraction of SJU from the SZHU stabilization unit, and the second inlet is with the supply line of circulating hydrogen from the hydroblock LNG fencing, the first input of which is connected to the hydrotreated broad fraction feed line of the NLF from the LNG hydrotreatment unit, the second input is connected to the purified hydrogen supply line from the hydrogen circulation unit, the third input is connected to the fourth fuel gas supply line from the hydrogen circulation unit, and the fourth input is connected with the supply line of the SZhT fraction 360-540 ° C for recycling from the SZhT fractionation unit, the first input of the SZhT fractionation unit being connected to the steam supply line from the water circulation unit, the second input to the fifth line of fuel g supply for from hydrogen circulation unit, and the third input - to a line supplying broad fraction SLF from block hydroforming SZHU, the purification unit of the synthesis gas from the CO 2 is output for CO 2 into the atmosphere, the hydrogen circulation unit has an output for supplying an excess of fuel gas to the factory network, the water circulation unit has an outlet for supplying excess steam from the water circulation unit to the factory network, and the SJT fractionation unit has the output of SJT fractions: “start of boiling” - 150 ° C, 150-180 ° C, 180-280 ° C, 280- 360 ° C and 360-540 ° C for their further use as fuel components .
RU2016112165A 2016-03-31 2016-03-31 Plant for producing synthetic liquid fuel RU2614956C1 (en)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU61278U1 (en) * 2006-10-05 2007-02-27 Открытое акционерное общество "Промгаз" (ОАО "Промгаз") Apparatus for producing synthetic liquid fuels (GTL) of coalbed methane
EA009247B1 (en) * 2004-03-19 2007-12-28 УОРЛД ДжиТиЭл, ИНК. A method and system for converting natural gas to liquid hydrocarbons
EA016088B1 (en) * 2005-12-30 2012-02-28 Юоп Ллк A process for producing light olefins, dimethyl ether and processing device for its realization
WO2013166583A1 (en) * 2012-05-09 2013-11-14 Expander Energy Inc. Enhancement of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment
RU2505475C1 (en) * 2012-05-24 2014-01-27 Открытое акционерное общество "НОВАТЭК" 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
WO2015012623A1 (en) * 2013-07-25 2015-01-29 대우조선해양 주식회사 Method and system for gtl production in fpso
EA021044B1 (en) * 2009-11-17 2015-03-31 Хемианлагенбау Хемниц Гмбх Method for generating hydrocarbons, in particular gasoline, from synthesis gas

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EA009247B1 (en) * 2004-03-19 2007-12-28 УОРЛД ДжиТиЭл, ИНК. A method and system for converting natural gas to liquid hydrocarbons
EA016088B1 (en) * 2005-12-30 2012-02-28 Юоп Ллк A process for producing light olefins, dimethyl ether and processing device for its realization
RU61278U1 (en) * 2006-10-05 2007-02-27 Открытое акционерное общество "Промгаз" (ОАО "Промгаз") Apparatus for producing synthetic liquid fuels (GTL) of coalbed methane
EA021044B1 (en) * 2009-11-17 2015-03-31 Хемианлагенбау Хемниц Гмбх Method for generating hydrocarbons, in particular gasoline, from synthesis gas
WO2013166583A1 (en) * 2012-05-09 2013-11-14 Expander Energy Inc. Enhancement of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment
RU2505475C1 (en) * 2012-05-24 2014-01-27 Открытое акционерное общество "НОВАТЭК" 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
WO2015012623A1 (en) * 2013-07-25 2015-01-29 대우조선해양 주식회사 Method and system for gtl production in fpso

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