Hydrogen sulfide-containing crude oil treatment

FIELD: crude oil treatment.

SUBSTANCE: treatment of hydrogen sulfide-containing crude oil before transportation and separation comprises multistep separation of original crude oil followed by dehydration and desalting, flushing with hydrocarbon gas in desorption column, and addition of monomethanolethanolamine (obtained by reaction of monomethanolamine with formaldehyde), and stirring. Flushing is accomplished with hydrogen sulfide-containing gas ensuring weight percentage of hydrogen sulfide in post-flushing oil no higher than 200 ppm. After addition of monomethanolethanolamine, according to invention, up to 10% of fresh washing water is additionally charged. All aforesaid operations are carried out before desalting step.

EFFECT: reduced contents of hydrogen sulfide and water in commercial oil.

1 dwg, 3 tbl

 

The proposal relates to a method of preparation of oil and can be used in the oil and gas industry in the preparation of hydrogen sulfide-containing crude oils, condensates with high content of hydrogen sulfide.

The known method of preparing fluids containing hydrogen sulfide oil, including its multi-stage separation, dehydration and desalting [Pozdnyshev G.N., Sokolov A.G. Exploitation of deposits and preparation of oil with a high content of hydrogen sulfide. Review, 1984, p.34-35].

The disadvantage of this method is that after the preparation of fluids containing hydrogen sulfide oil which has passed the separation at normal and elevated temperature is not achieved effective removal of hydrogen sulfide from crude oil and its contents in the produced oil does not meet the requirements of GOST R 51858-2002, according to which the mass fraction of hydrogen sulfide in crude oil shall not exceed 20 million-1(ppm).

The known method of preparing fluids containing hydrogen sulfide oil, including its multi-stage separation and Stripping purified hydrogen sulfide from the hydrocarbon gas in the limit separator when submitting 5-20 m3purified gas per 1 ton of oil and the temperature of the process of Stripping oil 30-70° [U.S. Pat. Of the Russian Federation No. 2071377, 01D 53/52, 19/00, publ. 10.01.97, bull. No. 1].

The disadvantage of this method is the lack of efficiency is removal of hydrogen sulfide from crude oil. After carrying out the processes of separation and Stripping oil residual content of hydrogen sulfide in crude oil does not meet the requirements.

There is a method of crude oil by multistage separation, Stripping hydrogen sulfide from crude oil in the desorption column gas not containing hydrogen sulfide, at a flow rate of gas Stripping 5-50 m3/m3oil [Leshin S. p. and other Basic directions of development of oil refining technology from hydrogen sulfide. J. Oil industry, 1989, No. 8, p.50-53].

The disadvantage of this method is that the process of Stripping of sour crude oil to reduce it the mass fraction of hydrogen sulfide up to 20 ppm is required to apply a large number of hydrocarbon gas (30-50 m3/m3), not containing hydrogen sulfide. Carrying out Stripping the oil with high specific flow rate of the hydrocarbon gas leads to lower output of crude oil due to the increased loss of valuable hydrocarbon, C4and higher gas Stripping.

Closest to the present invention is a method of preparing fluids containing hydrogen sulfide oil, including its multi-stage separation, dehydration and desalting, the Stripping of hydrocarbon gas in the desorption column, entering and mixing with monomethylethanolamine (MMEA) - a product of the interaction of monoethanolamine and formaldeh is Yes [U.S. Pat. Of the Russian Federation No. 2220756, 01D 19/00, 53/52, publ. 10.01.04, bull. No. 1].

A known method can reduce the mass fraction of hydrogen sulfide in crude oil up to 20 ppm with a combination of physical separation and Stripping of oil hydrocarbon gas in the column) and chemical (neutralization of hydrogen sulfide using MEA) methods for removing hydrogen sulfide from crude oil. While Stripping the oil is a hydrocarbon gas containing hydrogen sulfide, or natural gas to achieve a 90%degree of its purification from hydrogen sulfide and enter monomethylethanolamine, obtained by the reaction of monoethanolamine with 30-40%aqueous solution of formaldehyde in a molar ratio monoethanolamine:formaldehyde of 1:(1-4), is oil based 4-15 g per 1 g of the residual hydrogen sulfide and subsequent introduction into the oil-air, taken at the rate of 0.5 to 1.5 mol of oxygen per 1 mol of residual hydrogen sulfide after the process of desalination.

The disadvantage of this method is that when carrying out the Stripping fluids containing hydrogen sulfide oil gas not containing hydrogen sulfide, produce large amounts of sulfurous gas. The original design capacity of desulphurization (USO) is designed for volume sulfurous gas released in the process of oil separation at the booster nasanightlaunch (BPS) and system for the preparation of high-sulphur oil (UPVSN). The increase in revenues sulfurous gas USO reduce the degree of its purification from hydrogen sulfide and non-conformance with the requirements for the preparation of gas. When USO emergency or other situation for which there is no possibility of carrying out the process of gas purification from hydrogen sulfide, the hydrogen sulfide-containing gas coming from UPVSN and BPS for the installation of its preparation, is burned at the emergency torches. In this case, due to the lack of supply of gas not containing hydrogen sulfide, Stripping, desorption column is operated in the mode of separation (without gas for Stripping). As a result, significantly reduces the efficiency of removal of hydrogen sulfide from crude oil. To further bring the mass fraction of hydrogen sulfide in oil to values below 20 ppm requires the introduction of a large number of monomethylethanolamine, and in some cases air, which adversely affects the quality of the produced oil.

When carrying out the Stripping of oil from abnormally high mass fractions of hydrogen sulfide more than 2000 ppm of hydrocarbon gas, to achieve 90%removal of hydrogen sulfide, its content in the oil exceeds 200 ppm. Submission of monomethylethanolamine in oil with a residual mass fraction of hydrogen sulfide over 200 ppm after obeso the air traffic management of oil leads to a significant increase in the mass fraction of water in crude oil, and the resulting reaction products resulting from the interaction of monomethylethanolamine with hydrogen sulfide adversely impact analysis to determine the concentration of chloride salts in crude oil by the method GOST 51858-2002 (method And the titration of an aqueous extract), which manifests itself in the form of increased concentrations of chloride salts in oil.

It should be stated that the composition of crude oil, in addition to hydrogen sulfide, ethyl - and methyl mercaptans, also includes other elements and compounds (naphthenic acids, heavy mercaptans, phenols and the like), which can enter into chemical interaction with monomethylethanolamine. However, due to the occurrence of adverse reactions, neutralization of hydrogen sulfide in crude oil requires the introduction of monomethylethanolamine in excess of the desired value required for neutralization of hydrogen sulfide. When a high dosage of monomethylethanolamine possible a significant increase in the mass fraction of water in the crude product formed in a chemical reaction of hydrogen sulfide with formaldehyde, and bringing her with the reagent. In the known method, the mass fraction of hydrogen sulfide in oil after Stripping is 320 ppm. For neutralization of hydrogen sulfide in crude oil is introduced monomethylethanolamine, the resulting vzaimodeystvovat.primerno with a 40% aqueous solution of formaldehyde (formalin) in a molar ratio monoethanolamine:formaldehyde is 1:2,1 in number, equal to 8 g per 1 g of hydrogen sulfide. In this case, the mass fraction of water introduced with monomethylethanolamine in the process of neutralization of hydrogen sulfide in crude oil increases by 0.11%. Given that the first and second group of oil GOST 51858-2002 is the oil mass fractions of water, not exceeding 0,5%, bringing in such quantity as a result of the process of neutralization of hydrogen sulfide after the desalting process oil helps lower quality crude oil, and in some cases leads to a mismatch between the requirements of GOST R 51858-2002. Filing with the oil of air is taken as 0.5 to 1.5 mol of oxygen per 1 mol of residual hydrogen sulfide leads to lower output of crude oil due to the fact that to reduce DNP oil to regulate GOST R 51858-2002 values, according to which DNP commercial oil must not exceed 500 mm Hg, require subsequent separation of oil, in which the nitrogen of the air in the gas separation goes a considerable amount of heavy hydrocarbons.

The technical objective of the proposed method is to increase the quality of the crude product by reducing the mass fraction of hydrogen sulfide and water in the crude oil required to GOST R 51858-2002 values and avoid negative consequences of influence of the reaction products of MEA with Serov is gorodom in the analysis to determine the concentration of chloride salts in crude oil by the method GOST 21534-76 (method A - titration of an aqueous extract), increasing the degree of gas purification from hydrogen sulfide on USO by reducing admission to USO additional quantities of sulfurous gas, reduce costs associated with the preparation of fluids containing hydrogen sulfide oil.

The goal of the project described is solved by the method of preparation of fluids containing hydrogen sulfide oil, including its multi-stage separation, dehydration and desalting, the Stripping of hydrocarbon gas in the desorption column, entering and mixing with monomethylethanolamine - product of the interaction of monoethanolamine and formaldehyde.

What's new is that the Stripping of oil carry hydrogen sulfide-containing gas, providing the value of the mass fraction of hydrogen sulfide in oil after Stripping of no more than 200 million-1(ppm), and after entering monomethylethanolamine in oil additionally serves up to 10% of fresh wash water, and the processes carried out before the step of desalting.

The essence of the proposal is as follows.

The Stripping of oil is carried out at a temperature of 25-70°and the absolute pressure in the desorption column of 0.1-0.25 MPa hydrogen sulfide-containing gas, the flow which is observed to achieving the mass fraction of hydrogen sulfide in oil not more than 200 ppm. The expediency of use for Stripping oil gray is vodorodsoderzhashchee gas, providing the value of the mass fraction of hydrogen sulfide in oil after Stripping is not more than 200 ppm, related to the fact that the Stripping hydrogen sulfide from oil to this value as possible when submitting gas not containing hydrogen sulfide and when submitting sulfurous gas with a relatively low content. The Stripping oil hydrogen sulfide-containing gas can significantly reduce the receipt of the additional amount of sulfurous gas USO with the same amount of output of commodity oil compared using a gas not containing hydrogen sulfide.

Numerous field studies have established that the introduction of oil with a mass fraction of hydrogen sulfide more than 200 ppm of MEA after stage demineralization leads to an increase in the mass fraction of water in oil, and the reaction products of MEA with hydrogen sulfide has an adverse effect on the analysis of determining the content of chloride salts in crude oil by the method GOST 21534-76 (method And the titration of an aqueous extract), which manifests itself in the form of increased concentrations of chloride salts in the oil. Increasing the water content in the oil after the process of neutralization of hydrogen sulfide occurs as a result of bringing her with monomethylethanolamine and products of the reaction of hydrogen sulfide with MEA. Reduction, and in some cases elimination of consequences of influence is of the reaction products of MEA with hydrogen sulfide in the quality of commercial oil possible during the process of neutralization of hydrogen sulfide in oil before desalting. The process of desalination of oil after the chemical interaction of hydrogen sulfide with monomethylethanolamine and oxygen allows leaching of fresh wash water not only chloride salts, but also the reaction products of MEA with hydrogen sulfide, as well as to remove waste water introduced with monomethylethanolamine and reaction products. When this supply of fresh wash water in an amount up to 10% and the subsequent conduct of the desalting process oil must be done after complete chemical interaction of MMEA, oxygen and hydrogen sulfide. When applying the oil more than 10% of fresh wash water efficiency reducing the amount of chloride salts and water-in-oil rises slightly.

The proposed technological installation method of preparation of the fluids containing hydrogen sulfide oil presented in the diagram (see drawing).

The scheme includes the supply pipe 1 crude oil, oil separator 2, the first stage of separation, the oil separator 3 the second stage of separation, the installation of heating and deep oil dehydration 4, desorption column 5 gas 6 gas supply to the column, the pipeline 7 filing sulfurous gas USO, oil separator 8 low pressure mixer 9, the pipeline 10 filing MEA, site dispensing of MEA 11, the pipeline and/is whether the reactor 12, electrodesiccation 13, line 14 supply of fresh wash water piping 15 water drainage, pipeline 16 drain tank oil.

The method of preparation of fluids containing hydrogen sulfide oil is as follows.

Crude hydrogen sulfide-containing oil through the pipeline 1 is served in the separator 2, the first stage of separation. Then the oil through the separator 3 second separation stage is fed to the installation of heating and dehydration of oil 4, which is heated and deep dehydration of oil. Before Stripping the oil in the desorption column hydrogen sulfide-containing gas is held chromatographic analysis to determine the molar fraction of hydrogen sulfide in the hydrogen sulfide-containing gas supplied to the Stripping, and the use of this gas under specified conditions of preparation fluids containing hydrogen sulfide oil. After dehydration oil the hydrogen sulfide-containing gas is fed in the upper part of the desorption column 5. In the lower part of the desorption column through the pipeline 6 is fed hydrogen sulfide-containing gas, for example, with the first stage of separation. With desorption column hydrogen sulfide-containing gas through the pipeline 7 is fed at USO and oil through the low pressure separator 8 is supplied to the mixer 9. Before the mixer in the flow of oil through the pipeline 10 from node dosing of MEA 11 served monometallic elamin. In the mixer is efficient mixing of monomethylethanolamine with oil. Further, the oil enters the pipeline and/or the reactor 12 in which a chemical reaction interaction of hydrogen sulfide with MEA. After the process of neutralization of hydrogen sulfide oil enters electrodesiccation 13. Before the desalter in the oil through the pipeline 14 is served until 10% of fresh wash water for laundering of oil chloride salts and the products of the reaction of hydrogen sulfide with MEA. Water from the desalter through the pipeline 15 is supplied to cluster pumping station (SPS) for injection into the reservoir. With the desalter pipeline 16 commodity oil is supplied to surrender in the main pipeline.

Studies of the proposed method of preparation fluids containing hydrogen sulfide oil held in the laboratory.

Hydrogen sulfide-containing oil is selected after stage deep dehydration and heated to a temperature of 25; 40 and 70°With load in thermostatic model of the desorption column after its preliminary purging for 15 minutes petroleum gas not containing hydrogen sulfide. The purge gas is required to remove air from the model desorption column and prevent oxidation of sulfide by oxygen. The model of the desorption column is equipped with a filter SCHOTT equal to REGO gas distribution in the cross section model desorption columns and rings process. The process of Stripping the oil is carried out at an absolute pressure in the column is equal to 0.1; 0,12; 0.2 and 0.25 MPa. Through the filter of SCHOTT in the model desorption columns is served hydrocarbon gas with a molar fraction of hydrogen sulfide, 0.5; 0.8; 1; 1,5; 2; 3%. Specific gas consumption varies from 1 to 25 m3/m3oil to achieve mass fraction of hydrogen sulfide in oil not more than 200 ppm, which is periodically determined by sampling of oil from the model desorption columns and analysis to determine the mass fraction of hydrogen sulfide in oil. Hydrogen sulfide-containing gas released in the process of Stripping the oil is passed through two successive Drexel with a solution of cadmium acetate to hydrogen sulfide gas. For measuring the volume of gas Stripping using the gas meter. Loss of oil, gas Stripping is determined by weighing the oil on electronic scales. Research of process of Stripping are carried out with oil, selected on UPVSN NGDU "Nurlatneft and NGDU "Leninogorskneft" JSC "Tatneft". The density and dynamic viscosity of oil NGDU "Nurlatneft at a temperature of 20°To be 930 kg/m3and 300 MPa·s, respectively. The density and dynamic viscosity of oil NGDU "Leninogorskneft" at a temperature of 20°make 895 kg/m3and 40 MPa·respectively.

Conditions and results of research in the topic can be found in tables 1 and 2.

Hydrogen sulfide-containing oil with a mass fraction of water, equal to 2%, is loaded into the reaction flask and heated to a temperature of 40°C. Then the oil enter MMEA in a molar ratio monoethanolamine: formaldehyde of 1:4 of 7 g per 1 g of hydrogen sulfide. Next, the reaction mixture is stirred on a magnetic stirrer for 1 hour to conduct the process of neutralization of hydrogen sulfide in oil, after which it served 5; 10; 15% of fresh wash water and within 2 hours of the produce sucks (desalting) of oil with subsequent determination of sulfide, chloride salts and water in oil.

Conditions and results are shown in table 3.

Hydrogen sulfide-containing oil with a mass fraction of water, equal to 2%, is loaded into the reaction flask and heated to a temperature of 40°C. Further, in the oil serves 5; 10; 15% of fresh wash water and within 2 hours of the produce sucks (desalting) of oil, then enter MMEA in a molar ratio monoethanolamine: formaldehyde of 1:4 of 7 g per 1 g of hydrogen sulfide. Then the reaction mixture was stirred on a magnetic stirrer for 1 hour to conduct the process of neutralization of hydrogen sulfide in oil with subsequent determination of sulfide, chloride salts and water in oil.

Conditions and results are shown in table 3.

The data presented in that the faces 1 and 2, show that the receipt of the additional amount of sulfurous gas in the USO during the process of Stripping oil hydrogen sulfide-containing gas in the desorption column is significantly reduced with increasing viscosity and density of oil. It is established that with the increase of oil temperature and reduced pressure in the desorption column additional flow sulfurous gas from the desorption column and loss of oil, gas Stripping grow. In this regard, it is most expedient to carry out the Stripping of oil to the value of the mass fraction of hydrogen sulfide in oil not more than 200 ppm hydrogen sulfide-containing gas with a molar fraction of hydrogen sulfide, not exceeding 1.5% at a temperature of 25-50°and an absolute pressure of 0.1 to 0.12 MPa. Provided the need for Stripping the oil at higher temperatures equal to 50-70°and the pressure in the desorption column, close to atmospheric, do not exclude the possibility of Stripping oil hydrogen sulfide-containing gas with a higher molar proportion of hydrogen sulfide (e.g., the Stripping of oil NGDU "Nurlatneft in the desorption column is possible hydrogen sulfide-containing gas with a molar fraction of hydrogen sulfide, not exceeding 2%, to the value of its mass fraction in the oil is not more than 200 ppm at the temperature of the oil 70°and an absolute pressure of 0.1 MPa).

From this table the s 3, the introduction MMEA in oil to supply fresh water wash (up to demineralization), compared with the introduction of MEA in the oil after the filing of a fresh wash water after desalination), allows you to more effectively reduce the mass fraction of water in the crude oil and the effect of the negative influence of the reaction products of MEA with hydrogen sulfide in the analysis to determine the concentration of chloride salts in crude oil by the method GOST 21534-76 (method And the titration of an aqueous extract). Introduction MMEA in oil with initial mass fractions of hydrogen sulfide up to 200 ppm not have a significant negative impact on the quality of crude oil through the mass fraction of water and the concentration of chloride salts. The oil belongs to the first group, because, according to GOST R 51858-2002, mass fraction of water and the concentration of chloride salts in the oil do not exceed 0.1%, and 100 mg/DM3respectively. The supply of fresh water wash over 10% in oil is not advisable due to the fact that the mass fraction of water and the concentration of chloride salts in the oil is reduced slightly.

We offer a combination of physical (multi-stage oil separation, Stripping oil hydrogen sulfide-containing gas in the desorption column) and chemical (neutralization of hydrogen sulfide in oil MMEA) methods for removing hydrogen sulfide from crude oil during its preparation in the specified consistently the tee will allow you to:

- to improve the quality of crude oil by reducing the mass fraction of hydrogen sulfide and water in it to the required GOST R 51858-2002 values and avoid negative consequences of influence of the reaction products of MEA with hydrogen sulfide in the analysis to determine the concentration of chloride salts in crude oil by the method GOST 21534-76 (method And the titration of an aqueous extract);

to increase the degree of gas purification from hydrogen sulfide on USO by reducing admission to USO additional quantities of sulfurous gas;

- increase of trouble-free service life of equipment and pipelines by reducing hydrogen sulfide corrosion, to prevent pollution of sulfur compounds during transportation and storage of crude oil;

to reduce the costs associated with the preparation of fluids containing hydrogen sulfide oil to the requirements of GOST R 51858-2002, by reducing the metal content of the gas pipeline supply sulfurous gas from UPVSN to install its preparation and eliminating the need for laying additional pipeline transportation purified from hydrogen sulfide gas with the USO to UPVSN. The proposed method for the preparation of fluids containing hydrogen sulfide oil technologically advanced and simple in execution. It can be implemented on existing UPVSN and newly designed installations.

-
Table 1
The mole fraction of H2S in the gas supplied to the Stripping, %Temperature, °The absolute pressure in the column, MPaThe specific consumption of gas supplied to the Stripping, m3/m3oilMass fraction of H2S in oil after column, ppmAdditional amount of sulfurous gas delivered at the USO, m3/t oilLoss of oil, kg/t of crude oil
Oil NGDU "Nurlatneft"
H2S no250,161504,86-
0,1281455,98-
0,5250,16190--
0,128196--
0,8250,17200--
0,1210195--
1250,18190-
0,1213195--
1,5250,113200--
0,1220210--
2250,1252200,25
H2S no400,141504,050,29
0,1261305,38-
0,5400,14180-0,29
0,126165--
0,8400,14190-0,29
0,126190--
1400,15175-0,57
0,127185--
1,5 400,129200--
2400,182051,68
H2S no700,11,5140to 3.67of 5.68
0,261405,44-
0,257185of 5.06-
0,5700,11,51502of 5.68
0,26180--
0,259180--
0,8700,11,51552of 5.68
0,27180-0,45
0,2511190--
1700,11,51602of 5.68
0,28180- 1
0,2513190--
1,5700,11,51702of 5.68
0,211200-2,71
0,2520230-1,97
2700,11,51802of 5.68
3700,121802,32to 6.67

td align="center"> 7,38
Table 2
The mole fraction of H2S in the gas supplied to the Stripping, %Temperature, °The absolute pressure in the column, MPaThe specific consumption of gas supplied to the Stripping, m3/m3oilMass fraction of H2S in oil after column, ppmAdditional amount of sulfurous gas delivered at the USO, m3/t oilLoss of oil, kg/t of crude oil
Oil NGDU "Leninogorskneft"
H2S no250,1 41506,793,72
0,1251606,891,97
0,5250,141752.343,72
0,1251801,231,97
0,8250,141952,343,72
0,1271901,161,85
1250,151902,323,76
0,1272001,11,83
1,5250,182002,314,08
0,12202052,321
2250,182402,314,08
H2S no400,121506,176,46
0,123 1553,15,33
0,5400,121653,956,46
0,1231773,15,32
0,8400,121753,956,46
0,1231903,15,32
1400,121803,956,46
0,1232003,15,32
1,5400,121953,956,46
0,1252003,25,9
2400,152054,348,33
H2S no700,10,51167,8815,7
0,241307,827,3
0,257120 9,715,1
0,5700,10,51207,3815,7
0,241603,377,3
0,2571611,915,1
0,8700,10,51237,3815,7
0,241803,377,3
0,2571901,915,1
1700,10,51257,3815,7
0,241903,377,3
0,2582002,015,5
1,5700,10,51287,3815,7
0,262003,638,56
0,25102402,26,33
2700,10,513215,7
3700,10,51357,3815,7

15%
Table 3
The initial mass fraction (prior to entering MEA and wash water)The concentration of chloride salts in the original oil, mg/DM3Dosage of MMEA, g/g H2S (kg/t of oil)Mass fraction of H2S in commercial oil, ppmMass fraction of water in the crude product, %, during the introduction of MEAThe concentration of chloride salts in crude oil, mg/DM3when the introduction MAA
H2S, ppmWater %before filing a fresh wash water to the desalination)after the submission of the fresh wash water after desalination)before filing a fresh wash water to the desalination)after the submission of the fresh wash water after desalination)
5%10%15%5%10%15%5%10%5%10%15%
15021607 (1,2)180,60,40,380,90,870,85544038807572
20021607 (1,4)160,740,480,451,00,950,94826058958582
30021607 (2,2)90,960,80,751,31,251,22957066202193181
40021807 (2,8)181,00,90,851,41,31,251459078225218210

The method of preparation of fluids containing hydrogen sulfide oil, including its multi-stage separation, dehydration and desalting, the blow-off at levothrodi gas in the desorption column, entering and mixing with monomethylethanolamine - product of the interaction of monoethanolamine and formaldehyde, characterized in that the Stripping of oil carry hydrogen sulfide-containing gas, providing the value of the mass fraction of hydrogen sulfide in oil after Stripping of no more than 200 million-1(ppm), and after entering monomethylethanolamine in oil additionally serves up to 10% of fresh wash water, and the processes carried out before the step of desalting.



 

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1 dwg

FIELD: different branches of economy; the systems for purification of the biogas.

SUBSTANCE: the invention is pertaining to the field of the chemisorptive-catalytic purification of the biogas, in particular, to the chemisorptive-catalytic system for purification of the biogas. The system consists of: the stirring device (1)of the source biogas with the air and the part of the biogas purified from sulfur; the heater of the produced gas mixture (2); the reactor of oxidation of hydrogen sulfide (3); the heat exchanger for cooling of the gas mixture and condensation of the vapors of the formed elemental sulfur (5); the pipeline (8) for recirculation of the part of the biogas purified from sulfur; and, at least two parallel chemisorbers (6) with the fixed layers of the solid granular chemisorbent of the hydrogen sulfide (7). The reactor contains the fixed layer of the solid granular catalyst (4) for oxidation of hydrogen sulfide by oxygen up to the elemental sulfur. The device stirring device contains the control system of the air consumption and the part of the biogas purified from sulfur made with the capability to maintain the concentration of hydrogen sulfide in the produced gas mixture of no more than 1.2 volumetric % and the concentrations of oxygen within the range of 60-100 % from the indicated concentration of the hydrogen sulfide. The invention allows to reduce consumption of the chemisorbent and the volume of formation of the secondary wastes, to utilize the biogas with production of power and commercial products - the elemental sulfur, the high-quality carbon dioxide and to increase efficiency of purification of the biogas at the minimal capital expenditure and the operational costs.

EFFECT: the invention ensures: the reduced consumption of the chemisorbent and the volume of formation of the secondary wastes;, utilization of the biogas with production of power and commercial products - the elemental sulfur, the high- quality carbon dioxide; the increase efficiency of purification of the biogas at the minimal capital expenditures and the operational costs.

5 cl, 2 ex, 1 dwg

FIELD: gas-oil-producing and processing industry; methods and devices of purification of the gas containing hydrogen sulfide.

SUBSTANCE: the group of inventions is pertaining to the field of purification of the gas containing hydrogen sulfide and may be used in gas-oil-producing and processing industry. The method providing for purification of the gas containing hydrogen sulfide with extraction of sulfur by oxidizing the gas includes its contacting with the activated charcoal with the subsequent regeneration of the latter. Before contacting with the charcoal the oxidization is conducted by injecting of the dispersed oxygen saturated water into the purified gas, and the contacting with the charcoal is exercised for a short time. At that the activated charcoal is located on the rotating surface. The product of oxidation representing the suspension made out of the condensate, water and the elemental sulfur is subjected to flotation, and a part of the purified from hydrogen sulfide gas preheated and use in the process of flotation and regeneration. The installation for purification of the gas includes the block of oxidation, the block of saturation of the water with oxygen, the injector, on the outlet of which there is the screen with the filtering surface, the block of flotation, on the outlet of which there is the block of compaction of the elemental sulfur connected with the block of smelting, the accumulator of the liquid. The screen filtering surface has the layer of the activated charcoal and is made with the capability of rotation and regeneration by the heated gas of the back blowing. The block of saturation of water with oxygen is connected to an inlet of the injector, and the accumulator of the liquid is made with the capability of the three-phase separation into the water, the gaseous condensate and the gas degased from the liquid. The inventions ensure the increased service life of the installation, improvement of the quality of purification, the possibility to separate the condensate in the process of the purification and utilization of the products of the purification.

EFFECT: the inventions ensure the increased service life of the installation, improvement of the quality of purification, the possibility to separate the condensate in the process of the purification and utilization of the products of the purification.

15 cl, 1 dwg

FIELD: natural gas industry; petroleum industry; methods of combined purification of a natural gas and devices for its realization.

SUBSTANCE: the invention is pertaining to the field of natural gas industry and petroleum industry, in particular, to the methods and devices of combined purification of natural gases from acidic ingredients of a natural gas, a carbon dioxide, sulfur compounds. The mean includes two stages of a gas purification. In the beginning the initial gas is preliminary purified from acidic ingredients by absorption in the apparatus ensuring a contact of the subjected to purification gas with a chemical sorbent. Separate the absorbed acidic ingredients of the gas from the chemical sorbent in a desorber by its heating, then cool the chemical sorbent in a heat exchanger and pump in the absorber. At the second stage conduct deep purification and gas dewatering by adsorption by alternately operating adsorbers. At that absorption of the acidic ingredients is conducted in the screw compressor in the process of the gas compression. Into the working cavity of compression of the screw compressor feed the chemical sorbent, which is treated in an electromagnetic field with a flux density of 0.15-0.25 Tl. Desorption of the purification products is conducted in desorber under pressure of 0.8-0.9 bar (aeu - absolute electrostatic unit), formed by the water-ring vacuum pump, which simultaneously traps the water steam and chemical sorbent. The device for realization of the method is described also. The invention allows to increase the mass-transfer coefficient at the contact of the subjected to purification gas with the chemical sorbent, to reduce mass- overall dimensions of the combined purification unit and its materials consumption.

EFFECT: the invention ensures an increased mass-transfer coefficient at the contact of the subjected to purification gas with the chemical sorbent, reduced mass- overall dimensions of the combined purification unit and its materials consumption.

2 cl, 1 ex, 1 dwg

FIELD: gas treatment.

SUBSTANCE: invention relates to compositions for oxidative removal of hydrogen sulfide from gases to produce elementary sulfur, which compositions can be used in oil and gas production, petroleum and gas processing, chemical, and other industries. Absorbent contains, g/L: iron chelate compound (on conversion to ferric ion) 2-12, alkali metal phosphate (on conversion to phosphate anion) 1-16, alkali metal carbonate or hydroxide 1-60, methyldiethanolamine and/or triethanolamine 10-30, monoethanolamine/formaldehyde reaction product 0.2-10, and water to 1 L. Monoethanolamine interacts with 37% formaldehyde solution at molar ratio 1:(1-3). Iron chelate compound is a complex of ferric compound with ethylenediaminetetraacetic acid disodium salt. To reduce foaming, absorbent may further contain 0.05-0.2 g/L aluminum sulfate.

EFFECT: increased stability and decreased corrosive activity of absorbent without loss in its high absorbing capacity regarding hydrogen sulfide.

4 cl, 2 tbl, 5 ex

FIELD: gas treatment.

SUBSTANCE: invention is directed to remove hydrogen sulfide from CO2-containing process gases from enterprises involving heat treatment of sulfur-containing combustible fossils in reductive medium. Treatment comprises countercurrent contact of gases with liquid basic absorbent, absorption of hydrogen sulfide with absorbent, separating hydrogen sulfide from associated carbon dioxide, and converting hydrogen sulfide into usable products. Absorbent is selected from aqueous solutions or suspensions of alkali and alkali-earth metal hydroxides and oxides. Contact of gas with absorbent is performed in vortex chambers provided with rotating gas-liquid layer at residence from 0.001 to 0.1 sec.

EFFECT: increased degree of purification of gases and simplified treatment scheme.

1 dwg, 5 ex

The invention relates to processes of absorption and cleaning of gases from sulfur-containing impurities and can be used in the purification of gases of different composition

FIELD: oil refining industry; separation devices for transformation and-or treatment distillates and the liquid wastes of the oil refining technological process.

SUBSTANCE: the invention is pertaining to the field of oil refining industry and may be used for transformation and-or treatment distillates and the liquid wastes of the oil refining technological process. The device for separation of the mixture contains at least one gaseous phase and one liquid phase which are fed from the area of contact of the fluid fraction, the gaseous fraction and the solid particles. The device is disposed in the reaction chamber and contains: at least the tool (210) for recycling of the mixtures in the production cycle, which is supplied at least with one channel for the indicated mixture; one first component (280) for separation or the primary separator installed directly after one or several pipe ducts and allowing to provide fractionation of the mixture into the fraction (A) containing the dominating share of the liquid and the smaller share of the gas, and into basically gaseous fraction (B) containing the smaller share of the liquid; the pipe duct (70) disposed in the direct proximity of the upper part of the reaction chamber and ensuring possibility of removal of the fraction (B), fed from the primary separator; the pipe duct (30) used for the removal, which is continuation of the tool (210) for the mixture recycling, and through which under action of gravity the fraction (A) containing the dominating share of the liquid and coming out of the primary separator runs out and is removed. The device in addition contains the gear (130) to control the level of the liquid phase in the reaction chamber, and which configured so, that to keep this level at some spacing interval from the used for fraction (B) outlet opening, which exceeds or is equal to 0.05 of the value of the internal diameter of the reaction chamber. At that the fraction (B) is predominantly the gaseous. Besides the device may be supplied with at least one more separating component or the secondary inertia type separator (310) ensuring possibility of separation of the fraction (B) into the gaseous fraction removed by the pipe duct (70), and the liquid fraction removed by the pipe duct (30). The technical result of the invention is the improve process of separation of the mixture inside the reaction chamber, in which there are the gaseous fraction and the liquid fraction containing some random solid particles.

EFFECT: the invention ensures the improved process of separation of the mixture inside the reaction chamber, where there are the gaseous fraction and the liquid fraction containing some random solid particles.

16 cl, 4 dwg

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