The method of processing natural gas to methanol obtaining

 

(57) Abstract:

The invention relates to the chemical industry and can be used on units of production of methanol. The method of processing natural gas from the receipt of methanol, which includes stages of compression of natural gas, desulfurization, catalytic steam reforming with heat recovery converted gas, compressing the converted synthesis gas, methanol synthesis and distillation, is that the methanol synthesis is performed with an occasional change in the atmosphere of nitrogen upper catalyst layer within 0,5-1,75 warranty period of his service, the number of replacement catalyst is determined from the following dependence: Qlane= QI(A - 1)(B/C)nwhere Qlane- the number of overloaded catalyst, m3; QIthe number loaded into the reactor catalyst, m3; A - coefficient (1,15 - 1,27), dimensionless; B - coefficient of 1.65 and 1.75), wt.%; C - factor (0,9 - 1,1), wt.%; n is a constant (0,89), dimensionless. The technical result of the invention is to improve the utilization of natural gas and saving the methanol synthesis catalyst.

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A method of refining natural gas with methanol obtaining that includes the following basic stages:

compression of natural gas to 30 kg/cm2;

the desulfurization;

catalytic steam reforming of natural gas with steam in two parallel tubular furnaces with steam:gas ratio equal to 3:1, at a pressure of 30 kg/cm2and the exit temperature of 860oC;

waste heat recovery converted gas;

compressing the converted synthesis gas from 17 to 80 kg/cm2two-stage centrifugal compressor;

the synthesis of methanol in a single cycle with two parallel adiabatic reactors in which the catalyst is in four divided layers in the reference lattices, with the Central and peripheral mixers for mixing gases and temperature regulation, under the pressure of 80 bar and a temperature of 210-270oC by circulation scheme;

the distillation of crude methanol in one preliminary and two main columns.

As actuators, compressors, fans and smoke exhausters to tubular furnaces most pumps installed steam turbine (Constant technological regulation M-750, N 128516, Gubaha there is considerable irregularity of the fall of the activity of the catalyst as a result of mechanical damage and chemical decontamination. Intensive decrease in activity occurs in the first direction of gas flow layers of the catalyst, especially in the first layer, while the activity of the lower layers is quite high.

This disadvantage synthesis reactors leads to unsustainable consumption of natural gas or replacing the entire volume of the catalyst in the loss of activity of only the first layer.

The technical result of the invention is the increased usage of natural gas and saving the methanol synthesis catalyst.

This technical result is achieved by the proposed method of processing natural gas from the receipt of methanol, comprising compressing the source of natural gas, desulfurization, catalytic steam reforming with heat recovery converted gas, the compression ratio of the last and the synthesis of methanol in the columns of the synthesis in the presence of a catalyst with subsequent rectification, while the methanol synthesis is performed with an occasional change in the current of nitrogen upper layer of catalyst columns synthesis, the amount of which is determined by the formula:

Qlane=QI(A-1)(B/C)n,

where Qlane- the number of overloaded catalyst on the first shelf m3trisomy;

B - factor (1,65-1,75), wt.%;

C - factor (0,9-1,1), wt.%;

n is a constant (0,89), dimensionless,

preferably periodic replacement of the catalyst in the upper layer to perform within 0,5 - 1,75 warranty period of his service.

The claimed technical solution meets the patentability requirements of "Novelty", "Inventive step" and "Industrial applicability" as a collection of characteristics: periodic replacement in the nitrogen atmosphere of the first catalyst layer in each of the columns of the synthesis and the estimated number of replacement of the catalyst is determined according to the invention from the following dependencies:

Qlane. = QI(A-1)(V/C)n,

where Qlane- the number of overloaded catalyst on the first shelf m3;

QIthe number loaded into the reactor catalyst, m3;

A - factor (1,15-1,27), dimensionless;

B - factor (1,65-1,75), wt.%;

S - factor (0,9-1,1), wt.%;

n is a constant, dimensionless,

provide non - obvious result is the increased usage of natural gas and thus increase the production of methanol and save the methanol synthesis catalyst.

Example osushestvila all of the above stages: the desulfurization, catalytic steam reforming of natural gas with steam in two parallel tubular furnaces with steam:gas ratio equal to 3:1, at a pressure of 30 kg/cm2and the exit temperature of 860oC, followed by heat recovery converted gas compression up to 80 kg/cm2the synthesis of methanol in two columns, in which the catalyst is in four divided layers in the reference lattices, with the Central and peripheral mixers for mixing gases and temperature regulation, under the pressure of 80 bar and a temperature of 210-270oC by circulating circuit and the rectification of the crude methanol in one preliminary and two main columns, after a certain period of time (~8 years) extent of use of natural gas decreased to 95,02%. The content of CO and CO2began to meet at the entrance to the reactor of 3.75% to 2.65%, the output of 1.9% 1,65%. Small value of the temperature difference at the inlet into the first layer and exit points to the deactivation of the catalyst is in the first layer.

By calculation, the number of overloaded catalyst in each of the columns:

Qlane= QI(A-1)(V/C)n= 131 m3(1,25-1) (1,75%/1,08 %)0,89= 50,3 m3,

where Q
In = 1,75% wt. coefficient;

C = 1,08% wt. coefficient;

n = 0,89 dimensionless (constant).

After replacing part of the catalyst on the first top shelf of each reactor in a stream of nitrogen utilization of natural gas amounted to 96,15%. The content of CO and CO2accordingly, at the entrance to the reactor at 3.35% and 2.5%, the yield of 1.15% and 1.5%. The temperature on the first shelf, respectively on the inlet and outlet in the first reactor 208o--->260oWith the second reactor 208o--->265oC.

After replacing part of the catalyst on the first shelf of the synthesis reactors, the unit worked for 2 more years to complete replacement of the catalyst.

As follows from the above example, the degree of use of natural gas increased by 1.13%. Saving costly catalyst for methanol synthesis was ~17%.

1. The method of processing natural gas from the receipt of methanol, comprising compressing the source of natural gas, desulfurization, catalytic steam reforming with heat recovery converted gas, the compression ratio of the last and the synthesis of methanol in the columns of the synthesis in the presence of a catalyst followed by distillation, characterized in that the methanol synthesis is carried out from the first catalyst is determined by the formula:

Qtrans.= Qloading.(A - 1) (B / C)n,

where Qtrans.- the number of overloaded catalyst on the first shelf m3;

Qloading.the number loaded into the reactor catalyst, m3;

A - factor (1,15 - 1,27), dimensionless;

B - factor (1,65 - 1,75), wt.%;

C - factor (0,9 - 1,1), wt.%;

n is a constant (0,89), dimensionless.

2. The method according to p. 1, characterized in that the periodic replacement of the top layer of the catalyst is carried out for from 0.5 to 1.75 warranty period of his service.

 

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