The method of processing natural gas

 

(57) Abstract:

The invention relates to the processing of natural gas and can be used on plants to produce synthesis gas for methanol production. The method of processing natural gas includes the selection of natural gas, is heated in the tube space of the recuperation heat exchanger high-pressure heat circulating gas, dividing it into two streams in the ratio (75-85)/(25-15). Accordingly, the first thread bassereau, conduct catalytic steam reforming of obtaining the converted gas and waste heat last komprimiert, carried out the synthesis of methanol circulation unreacted gas and outlet purge gas, with heat recovery of unreacted gas and further cooled in an air cooler and refrigerator circulating water with separation of the condensed methanol. The second thread after throttling is used as fuel gas. After the compression of the converted gas is additionally passed through a heat exchanger-recuperator and isothermal flow reactor for methanol synthesis and purge gases are additionally passed through the expander is process. 5 C.p. f-crystals, 1 Il.

The invention relates to the processing of natural gas and can be used on plants to produce synthesis gas for methanol production.

A method of refining natural gas with methanol obtaining, including the selection of the source of natural gas from pipeline under pressure, throttling him, heating and split into two streams, one of which is used as fuel gas, and the other, the main thread, komprimiert to a pressure of 30 ATM and serves on stage desulfurization and then subjected to a process of catalytic steam reforming with heat recovery converted gas from separation from him and the condensed water, and the resulting synthesis gas is fed to the methanol synthesis after compression to a pressure of 80 ATM with subsequent heat recovery circulating gas, cooling it consistently air cooler and refrigerator circulating water, mechanical separation of methanol from neskondensirovannyh gases by distillation of crude methanol. (Constant technological regulation M-750, 128516, Gubakha, 1985).

The disadvantages of this method are the low yield of methanol from the unit about the inadequate condensation of methanol while cooling the circulating gas.

Closest to the proposed invention, the essence and the achieved technical result is the method of processing natural gas, including the selection of natural gas under pressure 30-45 MPa, then heated to 50oWith in the tube space of the recuperation heat exchanger high-pressure heat circulating gas with a temperature of 105-110oWith, dividing it into two streams in a volume ratio (75-85)/(25-15), respectively, the first of which serves to desulfurization, catalytic steam reforming of obtaining the converted gas and heat recovery last, kompremirovannyj, the synthesis of methanol circulation unreacted gas and outlet purge gas, with heat recovery circulating gas is further cooled in the air cooler and refrigerator circulating water with separation of the condensed methanol, and the second thread after throttling - on burning. (Patent RU 2124387 C1, prior. 22.03.98,, publ. 10.01.99,)

The disadvantages of the method are low yield of methanol per unit volume of the catalyst and increased energy consumption.

The technical result of the invention is to reduce energy costs and increase the efficiency of the process is m the selection of natural gas under pressure 30-45 ATM, the heat pipe in space recuperator heat exchanger high-pressure heat circulating gas, dividing it into two streams in a volume ratio (75-85)/(25-15), respectively, the first of which serves to desulfurization, catalytic steam reforming of obtaining the converted gas and heat recovery last, kompremirovannyj, the synthesis of methanol circulation unreacted gas and outlet purge gas, with heat recovery of unreacted gas and further cooled in an air cooler and refrigerator circulating water with separation of the condensed methanol, and the second thread after throttling - burning, in which, after the stage of compression of the converted gas is additionally passed through a heat exchanger-recuperator and isothermal flow reactor for methanol synthesis and purge gases from the methanol synthesis is additionally passed through the expander and heat exchanger purge gases and compressor expander is used to increase the pressure of the synthesis gas.

The technical result in the optimal level is achieved when the following conditions are met:

- the synthesis of methanol in isothermic parameter in the expander from 60-70 to 30-35 kg/cm2;

the cooled purge gas expander circulating gas separator before methanol to 15-25oC;

- the use of the compressor expander for the compression of the synthesis gas leaving the isothermal flow reactor and heat exchanger synthesis, to a pressure of 60-70 kg/cm2;

- heated natural gas in the tube space of the recuperation heat exchanger high pressure to 75-85oC.

The method is as follows.

The drawing shows a block diagram of the stepwise implementation of the method of processing natural gas.

Example.

Natural gas from the main gas pipeline under a pressure of 35 kg/cm2comes in tube space recuperator heat exchanger high-pressure 1, where it is heated to 80oWith the heat circulating gas fed into the shell side of the heat exchanger. After the heat exchanger 1, the gas is divided into two streams at a volume ratio of 80:20. Accordingly, the first thread cleaned of sulfur and sulfur compounds, which are poisons for catalysts conversion and synthesis, in the desulfurization reactor 3 after preheating in fire pre the conversion in two parallel tubular furnaces 4, where in the presence of Nickel catalyst vapor reacts with gaseous hydrocarbons under conditions of elevated temperature and pressure, forming a converted gas consisting of carbon dioxide, carbon monoxide, hydrogen, and residual (unreacted) methane.

Converted gas after reaction tube furnaces conversion 4 pass heat recovery 5, where the reduced temperature and separating the condensed water, is introduced to excess, the installation of the conversion. Heat the converted gas is used to produce steam, preheating boiler feed water, in the Department of rectification and heating demineralized water.

Dry the converted gas is compressed by the centrifugal compressor, the synthesis gas 6 driven by a condensing steam turbine with intermediate steam extraction and after the last stage of discharge is served in the recuperator heat of fusion 7 for heating the flow of gas emerging from the isothermal flow reactor for methanol synthesis 8, wherein the copper catalyst under a pressure of 57 kg/cm2and a temperature of 250oWith the formation of methanol. Due to the heat of fusion in isothermal flow reactor for methanol synthesis 8 p Coming out of the reactor 8 the synthesis gas through the heat exchanger 7 flows into the compressor 9 of the expander 10 and pressure of 65 kg/cm2included in the heat exchanger high pressure 1 for cooling to a temperature of 10oC. After the heat exchanger 1 is reacted in an isothermal flow reactor 8, the mixture is mixed with the cooled circulating gas from the main synthesis reactor 11, which is the synthesis of methanol at a temperature of 280oC and a pressure of 65 kg/cm2.

Circulating gas has a considerable excess of hydrogen, the degree of conversion of carbon oxides in a single pass over the catalyst of rectors of methanol synthesis is low, due to the approaching equilibrium concentrations of methanol and the original substances. After separation of the methanol synthesis in the output of the circulating gas contains a large amount of unreacted oxides of carbon returned to the synthesis loop. Continuous circulation of gases over the catalyst bed in the reactor 11 is carried out using a circulating compressor 12 driven by a condensing steam turbine.

Gas included in the methanol synthesis reactor 11, is heated in the recuperator heat of fusion 13 to the reaction temperature heat circulating gas leaving the synthesis reactor 11, the escaping coolant gas from the heat exchanger 13 at 108o<1 circulating gas from isothermal flow reactor 8. The mixed flow of the circulating gas from the isothermal flow reactor 8 and the reactor with cold chambers 11 is further cooled in heat exchanger purge gases 15 to 20oWith and into the separator methanol, 16.

In the separator 16 separates the liquid methanol, raw, and circulating the gas after separation of the methanol is returned to the suction side of the recirculation compressor 12, is heated in the heat exchanger 13 and the synthesis in the reactor 11. Part of the circulating gas after the separator are taken as purge gases, the pressure of which is reduced from 62 to 30 kg/cm2the expander 10, leaving the expander gases with a temperature of -5oWith heated in the recuperator 15 and fed to the combustion in the furnace conversion 4 and in the desulfurization reactor 3.

The second stream natural gas pipeline drossellied to a pressure of 8 ATM and used as fuel gas.

Due to the reaction of methanol synthesis in isothermal flow reactor increases, the yield of methanol per unit volume of the catalyst by 50%, reduced loading of the catalyst in an existing circuit synthesis by 40%, the reactions of methanol synthesis at lower westhuysen the case due to the drawdown of part of a gas in isothermal flow reactor to reduce the energy consumption for compression of the source and the circulating gas by 30% getting a pair in isothermal flow reactor reduces the production of steam in the existing boilers at 30%.

1. The method of processing natural gas, including the selection of natural gas under pressure 30-45 ATM, the heat pipe in space recuperator heat exchanger high-pressure heat circulating gas, dividing it into two streams in a volume ratio (75-85)/(25-15), respectively, the first of which serves to desulfurization, catalytic steam reforming of obtaining the converted gas and heat recovery last, kompremirovannyj, the synthesis of methanol circulation unreacted gas and outlet purge gas, with heat recovery of unreacted gas and further cooled in an air cooler and refrigerator circulating water with separation of the condensed methanol, the second thread after throttling - on combustion, characterized in that after the stage of compression of the converted gas is additionally passed through a heat exchanger-recuperator and isothermal flow reactor for methanol synthesis and purge gases from the methanol synthesis is additionally passed through the expander and heat exchanger purge gases and n is I, the synthesis of methanol in an isothermal flow reactor carried out under the pressure of 55-60 kg/cm2and a temperature of 230 to 270oC.

3. The method according to p. 1, characterized in that the pressure difference in the expander carried by up to 60-70 30-35 kg/cm2.

4. The method according to p. 1, characterized in that the purge gas from the expander is cooled circulating gas to the separator methanol to 15-25oC.

5. The method according to p. 1, characterized in that the compressor expander is used for the compression of the synthesis gas leaving the isothermal flow reactor and heat exchanger synthesis, to a pressure of 60-70 kg/cm2.

6. The method according to p. 1, wherein the natural gas is heated in the tube space of the recuperation heat exchanger high pressure to 75-85oC.

 

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FIELD: hydrocarbon conversion catalysts.

SUBSTANCE: catalyst for generation of synthesis gas via catalytic conversion of hydrocarbons is a complex composite composed of ceramic matrix and, dispersed throughout the matrix, coarse particles of a material and their aggregates in amounts from 0.5 to 70% by weight. Catalyst comprises system of parallel and/or crossing channels. Dispersed material is selected from rare-earth and transition metal oxides, and mixtures thereof, metals and alloys thereof, period 4 metal carbides, and mixtures thereof, which differ from the matrix in what concerns both composition and structure. Preparation procedure comprises providing homogenous mass containing caking-able ceramic matrix material and material to be dispersed, appropriately shaping the mass, and heat treatment. Material to be dispersed are powders containing metallic aluminum. Homogenous mass is used for impregnation of fibrous and/or woven materials forming on caking system of parallel and/or perpendicularly crossing channels. Before heat treatment, shaped mass is preliminarily treated under hydrothermal conditions.

EFFECT: increased resistance of catalyst to thermal impacts with sufficiently high specific surface and activity retained.

4 cl, 1 tbl, 8 ex

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