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  3. Designing the base of Driso ring and using hydrocarbon solvent in the dehumidification process in Farashband refinery.

Designing the base of Driso ring and using hydrocarbon solvent in the dehumidification process in Farashband refinery.

Number of pages: 103 File Format: word File Code: 31787
Year: 2011 University Degree: Master's degree Category: Chemical - Petrochemical Engineering
Tags/Keywords: BTEX compounds - Dehumidification - Drizo - Farashband Refinery - hydrocarbon solvent - impurity - TEG - The base of Driso's ring - water vapor
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  • Summary of Designing the base of Driso ring and using hydrocarbon solvent in the dehumidification process in Farashband refinery.

    Master's Thesis in Chemical Engineering

    Abstract

    Design of Driso ring base and use of hydrocarbon solvent in the dehumidification process in Farashband Refinery

     

    Water vapor is one of the most important impurities in natural gas flow. Usually, the water vapor itself is not a problem, but instead the liquid or solid phase that forms when the gas is compressed or cooled is a problem. In some cases, water vapor causes severe poisoning of expensive catalysts or causes adverse side reactions. Liquid water usually accelerates corrosion, and ice or solid hydrates can clog valves, fittings, and even gas pipes. To avoid such problems, the gas flow is dewatered using different methods before entering the transmission lines. The most common method in the world is the use of TEG. In order to increase the efficiency of the mentioned method, various things have been proposed, one of which is to add hydrocarbon solvent to TEG, which helps the volatilization of water in this solution in the removal tower and results in obtaining a purer TEG, and the dew point of the gas can be much lower than the currently used method. whose technology is now the monopoly of Drizo company and is known as the Drizo process, and by using the mentioned method, the purity of the TEG output from the disposal tower can be increased to more than 99.8%, and as a result, the dry gas with a dew point of -73 to -95.5 is transferred to the consumption points.

    triethylene glycol and prevent the release of BTEX compounds.

    Key words: Drizo, TEG, dehumidification, hydrocarbon solvent, BTEX compounds

    Natural gas dehumidification

    Raw gas [1] which is extracted from hydrocarbon reservoirs, is different from the gas that is sent to pipelines for consumption. In addition to methane, natural gas extracted from hydrocarbon reservoirs contains various impurities, which are separated during the natural gas refining process. Table (1-1) shows the impurities in natural gas[1]. One of these impurities is water vapor in natural gas. Figure (1-1) shows a view of the configuration of a gas refinery [2]. The position of the dehumidification unit in a gas refinery is known in this figure.

         The presence of water in natural gas, if the pressure increases to a certain level or the temperature decreases, causes the formation of gas hydrates. Accumulation of gas hydrates in the joints related to transmission or process pipelines or equipment, causes blockage of pipelines and increases corrosion. Gas hydrates are light and porous like snow and have a crystalline structure and multiply like crystal particles [3]. The ratio of water molecules to gas molecules is 5:75 for methane and 7:67 for ethane[4]. Figure (1-2) shows two crystal lattices related to hydrate.

    1-1-1- Natural gas dehumidification methods

    There are various methods for natural gas dehumidification, the most important of which are here
    From: [5].

    1- Dehumidification by moisture absorbent liquids[2] such as glycols[3].

    2- Dehumidification using solid absorbents[4] such as alumina gel[5], silica gel[6] and bauxite[7].

    3- Dehumidification by gas cooling [8].

    4- Dehumidification using gas penetration in the membrane.

    5- Dehumidification by solid reagents such as solid calcium chloride.

    Table (1-1): Impurities in natural gas[1]

    Principal Gas Phase Impurities

    Hydrogen sulfide

    Carbon dioxide

    Water vapor

    Sulfur dioxide

    Nitrogen oxide

    Volatile organic compounds(VOCs)

    Volatile chlorine compounds(e.g., HCL, CL2)

    Volatile fluorine compounds(e.g., HF, SiF4). style="direction: rtl;"> 

    Figure (1-1): A view of the configuration of a gas refinery [1]

    Figure (1-2): Two crystalline networks related to hydrate [3]

     

    1-1-1-1-Dehumidification by absorbent liquids Moisture

    The most common method for natural gas dehumidification is dehumidification using moisture absorbent liquids. Figure (1-3) shows a simple view of natural gas dehumidification process. Table (1-2) shows the characteristics of glycols used in the gas dehumidification process [1]. Among the four types of glycol given in this table, triethylene glycol (TEG) is the most suitable. The advantages of TEG compared to other glycols are:

    1- Lower vapor pressure compared to lighter glycols and as a result less wastage during regeneration.

    2- Higher resistance to heat decomposition [9] compared to lighter glycols and as a result higher purity of regenerated glycol.

    3- lower viscosity compared to T4EG.

         Adsorption with the help of triethylene glycol (TEG) is the most used method in separating water from gas. The inlet gas of the unit initially enters a separate vertical scrubber [10]. In this tool, any type of liquid in the gas is separated. At the entrance of this cleaner, an inclined guide is installed, which creates a rotating flow around the wall of the cleaner. (Rotational separation [11]) The wet gas at the outlet of the cleaner passes through a stainless steel dust collector [12] with a metal mesh and with high capacity and efficiency. This action is done to prevent any liquid particles from being carried by the gas. Then the gas enters the tower from below and passes around the tower. This tower can have a valve tray or bubble cap tray or it can be full. In this tower, the gas is placed in contact with the light glycol that entered from the top of the absorption tower. After the absorption section on top of the trays or the filling section, there is a space inside the tower for settling and return of droplets or impurities along with the gas. so that most of the droplets and particles of glycol settle in this part. If there is no sedimentation, all these drops and dusts will be taken by passing through the dust collector with a high efficiency considered at the top of this section, and the dry gas will exit from the upper end of the tower.

         The light and dry glycol entering the tower, which was exited from the overflow tank[13], is cooled in a converter before entering the tower to create maximum contact efficiency. The concentrated (light) glycol pressure of the overflow tank output reaches the operating pressure of the absorption tower by the pump. Glycol enters the contact tower and falls on the first tray. And then it comes in contact with the incoming wet gas with the counter flow and travels to the end of the tower. The wet, rich glycol that has now absorbed the gas water vapor exits the bottom of the tower and enters a high pressure glycol filter. This filter captures any foreign solid particles that may be carried by the gas stream before entering the next steps and the glycol pump. This is the ideal spot for the initial glycol filtration. After this filter, the rich glycol from the condenser coil and the flash tank, where the dissolved gases are removed, enters the glycol-glycol exchanger before the regeneration section. The warm rich glycol enters the lower part of the regeneration column. This tower is full and usually of Ceramic Saddle type.

  • Contents & References of Designing the base of Driso ring and using hydrocarbon solvent in the dehumidification process in Farashband refinery.

    List:

    The first chapter: Introduction

    1-1- Dehumidification of natural gas. 2

    1-1-1- Natural gas dehumidification methods. 2

    1-1-1-1- Dehumidification by moisture absorbent liquids. 4

    1-1-1-2- Dehumidification using solid absorbents. 6

    1-1-1-3- Dehumidification by gas cooling. 6

    1-1-1-4- Dehumidification using gas penetration in the membrane. 6

    1-1-1-5- Dehumidification by solid reagents. 7

    1-1-2- Methods of increasing the efficiency of the regeneration process. 10

    1-1-2-1- Use of repellent gas. 10

    1-1-2-2- vacuum recovery. 10

    1-1-2-3- Increasing the reduction action by adding solvent. 11

    The second chapter: Review of previous researches

    Review of previous researches. 13

    The third chapter: Increasing the action of glycol regeneration by adding hydrocarbon solvent

    3-1-Process specifications. 17

    3-2- The advantages of Driso.. 20

    3-2- 1- From an economic point of view. 21

    3-3- Modification of Drizo gas dehumidification process. 21

    3-3-1- Describing the modification of the Driso process. 22

    3-4- Design parameters. 22

    Title Page

    3-4-1- Contactor tower. 23

    3-4-2- inlet gas flow rate. 23

    3-4-3- Inlet temperature and pressure. 23

    3-4-4- temperature and concentration of TEG input. 23

    3-4-5- Glycol rotation speed. 24

    3-4-6- Dehumidification temperature. 24

    3-4-7- Reboiler temperature. 24

    3-4-8- The temperature of the disposal column. 24

    Chapter four: Basic design and provision of preliminary engineering services for the implementation of the Drizo project in the Farashband gas refinery, Dalan unit

    4-1- Based on the summer conditions and when the units are separate. 27

    4-1-1- three-phase separator (V-100). 27

    4-1-2- E-100 heat exchanger. 30

    4-1-3- heat exchanger E-101. 41

    4-1-4- Chiller that supplies cold water. 57

    4-1-5- P-100 pump. 60

    4-1-6- pipelines for transferring flow in Drizo process. 65

    4-2- Based on winter conditions and when the units are separate. 68

    4-2-1- three-phase separator (V-100). 68

    4-2-2- E-100 heat exchanger. 68

    4-2-3- heat exchanger E-101. 73

    4-2-4- Chiller that supplies cold water. 78

    4-2-5- P-100 pump. 80

    4-2-6- Pipelines for transferring flow in Drizo process. 81

    4-3- Based on summer conditions and in case of combining units. 82

    4-3-1- three-phase separator (V-100). 82

    4-3-2- E-100 heat exchanger. 82

    4-3-3- heat exchanger E-101. 87

    4-3-4- Chiller for supplying cold water. 92

    Title

    4-3-5- P-100 pump. 94

    4-3-6- pipelines for transferring flow in Drizo process. 95

    4-4- Based on winter conditions and in case of consolidation of units. 96

    4-4-1- three-phase separator (V-100). 96

    4-4-2- E-100 heat exchanger. 96

    4-4-3- heat exchanger E-101. 101

    4-4-4- Chiller that supplies cold water. 106

    4-4-5- P-100 pump. 108

    4-4-6- Pipelines for transferring flow in Drizo process. 109

    4-5-Separating water from the solvent ((coalesce). 110

    Chapter Five: Conclusion

    5-1-Comparison of the rate of TEG waste. 112

    5-2-Comparison of the emission rate of BTEX compounds. 113

    3-Comparison of the purity of TEG in the disposal tower.

    5-Comparison of the dew point of the dry gas exiting the absorption tower.

    5-Comparison of the total investment cost (TCI) due to

    implementation of the Drizou process in two cases. 116

    Resources

    1. A. L. Kohl, R. B. Nielsen, (1997). Gas Purification, Houston, Texas.

    2. Natural Gas Refining in the WikipediaNatural Gas Refining in the Wikipedia The Free Encyclopedia

    www.wikipedia.com.

    3. A. Rojey, C. Jaffret, (1997). Natural Gas Production Processing Transport, Editions Technip, Paris.

    4. Beijing Zehua Chemical Engineering Co., Ltd, (2006) “Sepak 250Y catalogue”. Beijing, China, http://www.zehua-chem.com [2007].

    5. J.M. Campbell, (1984). Gas Conditioning and Processing. Canada: Petroleum series.

    6. J. M. Campbell, (1982). Gas Conditioning and Processing. Vol. 1

    7. J. M. Campbell, (1982). Gas Conditioning and Processing. Vol. 2

    8. J. M. Campbell, (1982). Gas Conditioning and Processing. Vol. 3

    9. J. William Shell, (1982).” Spiral-wound permeators for purification and recovery.” Journal of Chemical Engineering Processing, October, pp. 33.

    10. A. Rojey, J. Claude, (1997). Natural Gas Production Processing Transport. Paris: Editions Technip.

    11. Gas Process Supplier's Assoc. (GPSA), (1987), Engineering Data Book Vol. II, Sec. 20, Tenth edition, Tulsa, OK.

    12. R. N. Maddox, L. L. Lilly, M. Moshfeghian, and E. Elizondo, (1988) “Estimating Water Content of Sour Natural Gas Mixtures, Proc. Laurance Reid Gas Conditioning Conf, University of Oklahoma,

    Norman, OK, p. 75.

    13. Z. Diaz, P. Nasir, and C. R. Wallace, (1991), Fundamentals of CO, Dehydration, presented at the 1991 AIChE Spring National Meeting, April 1-1 1, Houston, TX.

    14. P. Wieninger, (1991), "Operating Glycol Dehydration Systems, Proc. Laurance Reid Gas Conditioning Conference, University of Oklahoma, Norman, OK, p. 23.

    15. F. S. Manning, R. E. Thompson, (1991), Oilfield processing of petroleum, Volume one: Natural gas, Pennwell, p. 149.

    16. J.R. Cunningham, J.E. Coon, C.H. Twu, Estimation of aromatic hydrocarbon emissions from glycol dehydration units using process simulation, in: Proceedings of the 72nd Annual Gas Processors Association Convention, San Antonio, TX, March 15–17, 1993.

    17. W. P. Parrish, Won, and M. E. Baltatu, (1986), "Phase Behavior of the Triethylene Glycol-Water System and Dehydration/Regeneration Design for Extremely Low Dew Point Requirements, presented at the 65th Annual GPA Convention, March 10-12, San Antonio, TX.

     

    18. M. Herskowitz, M. Gottlieb, J. Chem. Eng. Data 29, (1984) 173–175.

    19. B. Bestani, K.S. Shing, Fluid Phase Equilibr. 50, (1989) 209–221.

    20. GPA Editorial Review Board, Recent developments in gas dehydration and hydrate inhibition, in: Proceedings of the Laurance Reid Conference, Norman, Oklahoma, 1994.

    21. S.K. Gupta, B.S. Rawat, A.N. Goswami, S.M. Nanoti and R. Krishna, Fluid Phase Equilibrium, 46, (1989) 95-102.

    22. R. S. Smith and T. B. Skiff, (1990), Drizo Gas Dehydration, Solution for Low Dew PointsfAromatics Emissions, Proc. Laurance Reid Gas Conditioning Conf, University of Oklahoma, Norman, OK, p. 61.

    23. C.H. Twu, W.D. Sim, V. Tassone, Fluid Phase Equilibr. 65–74 (2001) 183–184.

    24. C.H. Twu, W.D. Sim, V. Tassone, Fluid Phase Equilibr. 194–197 (2002) 385–399.

    25. H. Twua Chorng, Tassoneb Vince, D. Simb Wayne, Watanasiric Suphat, Advanced equation of state method for modeling TEG–water for glycol gas dehydration, Fluid Phase Equilib 228–229, (2005) 213–221.

    26. G. K. Foals, G. M. Kontogeorgis, M. L. Michelsen, E. H. Stenby, E. Solbraa, J. Chem. Eng. Data 2006, 51, 977-983.

    27. A. Fowler, (1975), "Super-Drizo, the Dow Dehydration Process." Proc.Gas conditioning Conf., 25th Annu, Mar 3-5 1975, University of Oklahoma, Norman, OK.

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    29. E. ?i. Lars, T. Selst? Elisabeth," PROCESS SIMULATION OF GLYCOL REGENERATION" for presentation at GPA Europe's meeting in Bergen 13th - 14th May 2002.

    30. T. Skiff; A Szuts; V Szujo; "A Toth"

Designing the base of Driso ring and using hydrocarbon solvent in the dehumidification process in Farashband refinery.
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