621.928.622.279 Recently, there have been attempts to explore and utilize low-yield deposits of natural gas which can play an important role in gasification of regions far away from main transmission gas lines.To prepare natural gas in such deposits, the Central Design Bureau Holding Company developed low-temperature separation (LTS) equipment for use in low-yield deposits with a productivity with respect to gas of 40,000 to 150,000 m3/day at a liquid content in the gas of up to 200 cm3/m 3. Equipment ( Fig. 1) consists of units required for preparing the gas by the method of low-temperature separation and includes the step I separator, the gas-gas heat exchanger, the step II separator, the divider, the ejector, regulation, closing, and safety fittings, and impeetion and monitoring devices.Taking into account the low productivity, the LTS equipment is assembled in the form of a single transport unit weighing 11.3 t, 9 m long, 2.4 m wide, and 2.8 m tall.Equipment consists of three main parts: stage I separation section, divides the section, and the stage II separation section.The stage I separation section (stage I separator) consists of a horizontal liquid collector with an internal diameter of 600 mm which contains an elliptical end on one side and a flange on the other side, and a head part 300 mm in diameter in which a mesh baffle of three centrifugal elements are placed for cleaning the gas.The dividing section (divider P-l) has the form of a coil whose two ends have flanges; inside the coil there is a moveable and changeable packed layer which uses inclined sheets to intensify the process of separation of the mixture (hydrocarbon condensate and methanol water) into components.The stage II separation section (stage II separator) consists of two horizontal containers: a liquid collector with an internal diameter 600 ram made in the same manner as the collector of the stage I separation section, and a separator with an outer diameter of 219 mm in which one centrifugal element is placed along the path of the gas flow.Using flanges separated by flat barriers, all sections are connected into a single apparatus. The barriers are designed for the total gas pressure gradient between the zones.The gas-gas heat exchanger is a horizontal apparatus with an outer diameter 325 mm with a U-shaped bundle of pipes 25 • 2 mm in diameter and 4 mm long. A special feature of this apparatus is that the "hot n flow is supplied at the bottom, and the "cold" flow at the top.A crude gas with a temperature of 4"C is supplied under a pressure of 7.9 MPa into the stage I separator where the drip liquid is separated from it and is then directed through the dispersion and methanol supply section into the gas-gas exchanger for cooling. The cooled gas travels through the regulating valve into the ejector and then travels to the stage II separator under a pressure of 5.7 MPa at a temperature of -25~Passing through the centrifugal element, the gas is directed into the space between the pipes in the heat exchanger where it is heated up and ...
An important task for the designers of new plant is the economic enhancement of equipment based on fumace heating and intermediate heating media.Basic geometrical and other parameters have been given [1--4] for two plants having furnace heating, which differed in the disposition of the heat-uptake tube bundles: in the old design, they were contained in a rectangular box above a cylindrical body, while in the new one, they were placed between the gas tubes (the rectangular box was eliminated, and consequently the hot outer surface was substantially reduced).The technological efficiency is a basic parameter governing the economic operation, and it can be defined by the foliowing if the fuel is gaseous: 1"1 a = 100 -(q2 + q3 + q5), (i) in which q2, q3, and q5 are the heat losses with the stack gases, due to incomplete combustion, and from the hot components into the surrounding space, respectively.It has been found [1, 2] that if the excess air factor in the fire tubes is c~ > 1.5, then q3 = 0, and (1) simplifies to qa = 100 -(q2 + qs)"The heat lost with the stack gases q2 is substantially dependent on the gas temperature ts:Vscsts-aV~176 100, q2-Qtp.in which V s = VRO 2 + V~ 2 + VI_t20 + (c~-I)V ~ is the stack gas volume; VRO 2, V~ VH20, V 0 are the volumes, respectively, of the triatomic gases, the nitrogen (theoretical), the water vapor, and the air (theoretical); c s is the average specific heat of the outgoing combustion products; (Ct)o is the product of the specific heat and temperature for the surrounding air; and Q~ is the available heat from the fuel.We compared q2 for the old and new plants in relation to the energy produced BQ~. = 20, 50, 100, 140 kW (where B is the fuel flow rate).
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Foreign practice and domestic experience with oil and gas production on the continental shelf indicate that the technicoeconomic indicators of the rigging and operation of deep-water platforms should be improved in the following directions:an increase in the number of wells per group to reduce the overall number of platforms in the field; multistory arrangement of production equipment on the platforms for well drilling and the recovery, collection, and preparation for transport of well production; use of automated assembly-unit equipment and its arrangement in unit modules to industrialize and reduce the time required for construction-assembly operations; and, broad implementation of automation and telemechanization of production processes to improve the safety of working conditions and fire safety.The most expedient production scheme for installations used in the preparation and transport of production to shore structures (SS) is determined as a function of the individual characteristics of each gas, gas-condensate, and oil field -the geographical location, depth of water, distance to the shoreline, the initial stratal pressure, the composition and physicochemical properties of the raw material, and the natural-chemical conditions. Three stages of gas processing are carried out.First. The gas is partially treated on the platform; this consists in extracting water vapor and a portion of the heavy hydrocarbons from the gas. The gas and condensate flows are fed through separate lines to the shoreline, where their further treamaent is carried out. In that case, short distances from the shore and a relatively even bottom relief are desirable. The alternate scheme in question permits the formation of a liquid phase in the gas pipeline from platform to shore.Second. The gas is treated on the platform, i.e., deep extraction of water and heavy hydrocarbons from the gas. The dew point of the gas with respect to those of the water and hydrocarbons ensures operation of gas lines in a virtually dry regime.Third. Water is separated from the stratal production. The gaseous and liquid hydrocarbon phases are then transported together to the shoreline.The production schemes of these installations differ little from the schemes of similar installations operating in normal fields on dry land. Quality gas indicators are obtained using the minimum required number of production techniques for a certain operating regime.The extent to which the condensate is treated in these installations is determined by the method of its transport, which depends on the amount of condensate, the distance between the platform and shoreline, the production life of the fields, etc. Depending on these factors, the mixture of liquid hydrocarbons can be stabilized to commercial condensate in conformity with OST 51.65-80 or subjected to partial degassing.Considering the high cost of production areas on a standard off-shore platform (SOP), and also the large outlays for production processes involving preparation of the raw material for transport, production op...
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