{"id":2109,"date":"2015-06-01T00:00:59","date_gmt":"2015-06-01T05:00:59","guid":{"rendered":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/?p=2109"},"modified":"2015-06-01T00:00:59","modified_gmt":"2015-06-01T05:00:59","slug":"effect-of-chemical-additive-on-crude-oil-pipeline-pressure-drop","status":"publish","type":"post","link":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/2015\/06\/effect-of-chemical-additive-on-crude-oil-pipeline-pressure-drop\/","title":{"rendered":"Effect of Chemical Additive on Crude Oil Pipeline Pressure Drop"},"content":{"rendered":"

For transportation of crude oil, the pumping power requirement varies as the crude oil viscosity changes. Increasing \u00b0API or line average temperature reduces the crude oil viscosity. The reduction of viscosity results in higher Reynolds number, lower friction factor and in effect, lower pumping power requirements.<\/span><\/p>\n

In the March 2009 tip of the month (TOTM), procedures for calculation of friction losses in oil and gas pipelines <\/b>were presented. The sensitivity of friction pressure drop with the wall roughness factor was also demonstrated. In the August 2009 TOTM, we also demonstrated the effect crude oil \u00b0API and the pipeline average temperature on the pumping requirement.<\/span><\/p>\n

In practical situations, an originating station takes crude out of storage and the midline stations taking suction from the upstream section of pipeline. Oil in the tank is often at ambient temperature, whereas once in the pipeline, the oil cools (or warms) to the same temperature as the ground. \u00a0In some parts of the world, the tank might be at +38 \u00b0C (+100 \u00b0F). \u00a0The first midline pumping station could operate at 18 \u00b0C (65 \u00b0F), and all subsequent pumping stations might operate at ground temperature, or notionally 9 \u00b0C (48 \u00b0F) with some seasonal variation. Therefore, a sound pipeline design should consider expected variation in crude oil viscosity which is normally a function of crude oil \u00b0API, and the line average temperature. In addition to \u00b0API and temperature, chemical additives may also affect crude oil pipeline pressure drop.<\/span><\/p>\n

To reduce pressure drop and increase pipeline capacity, oil industry has utilized drag reducing agents. Drag-reducing agents<\/b>, or\u00a0drag-reducing polymers<\/b>, are additives in pipelines that reduce\u00a0turbulence<\/span><\/a>\u00a0in a pipe. Usually used in\u00a0petroleum<\/span><\/a>\u00a0pipelines<\/span><\/a>, they increase the pipeline capacity by reducing turbulence and therefore allowing the oil to\u00a0flow<\/span><\/a>\u00a0more efficiently [1]. In addition to drag reducing agents, another group of chemicals called \u201cIncorporative Additives\u201d, which reduces crude oil viscosity, may be used. Halloran presented a series of general reading articles on chemical additives [2-4].<\/span><\/p>\n

In this TOTM, we will demonstrate the effect of an incorporative additive on crude oil viscosity and consequently on pressure drop for crude oil pipeline transportation.<\/span><\/p>\n

Case Study: Part 1 \u2013 Viscosity Reduction<\/b><\/span><\/p>\n

The laboratory measured kinematic viscosity for different <\/span>\u00b0API crude oil samples without<\/i><\/b> and with<\/i><\/b> \u201cIncorporative Additive\u201d at 50 \u00b0C (122 \u00b0F) reported by Oil Flux Americas [6] are shown in Table 1. The calculated density, absolute viscosity and percent reduction in viscosity for each oil sample at 50 \u00b0C (122 \u00b0F) are also shown in this table. As noted in this table, the lower \u00b0API (heavier oil), the greater the reduction in oil viscosity. <\/span>The measured kinematic viscosities as a function of crude oil <\/span>\u00b0API are shown in Figure 1. The absolute viscosity is calculated by multiplying the measured kinematic viscosity by density. The corresponding calculated absolute viscosities are also shown in Table 1 for crude oil samples \u201cWithout\u201d and \u201cWith\u201d additive, respectively.<\/span><\/p>\n

Table 1. Measured kinematic viscosity [6] and absolute viscosity for several crude oil samples at 50 \u00b0C (122 \u00b0F) without and with chemical additive.<\/span><\/p>\n

\"table1\"
cSt = (mm)2\/s cP = Poise\/100 = Pa.s\/1000 =kg\/m-s\/1000 = 0.000672 lbm\/ft-sec * Used in the case studies<\/figcaption><\/figure>\n
\"Figure
Figure 1. Effect of chemical additive on crude oil absolute viscosity at 50\u00b0C (122 \u00b0F)<\/figcaption><\/figure>\n
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The absolute viscosities (\u03bc) at 50 \u00b0C (122 \u00b0F) are fitted to a quadratic equation as follows:<\/p>\n

\"equations1\"<\/p>\n

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The absolute viscosities and the fitted correlations are shown in Figures 2 and 3 for crude oil samples \u201cwithout\u201d and \u201cwith\u201d chemical additive, respectively.<\/p>\n

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Case Study: Part 2 \u2013 Pressure Drop Calculations<\/strong><\/p>\n

For a case study, we will consider a 55 km (34.18 miles) pipeline with an outside diameter of 406.4 mm (16 in) carrying crude oil with two separate flow rates of 7,950 and 15,900 m3\/d (50,000 and 100,000 bbl\/day). The wall thickness was estimated to be 5.7 mm (0.225 in). The wall roughness is 46 microns (0.0018 in) or a relative roughness (\u03b5\/D) of 0.0001. The procedures outlined in the March 2009 TOTM were used to calculate the line pressure drop due to friction. Since the objective is to study the effect of incorporative chemical additive, we will ignore elevation change.<\/p>\n

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It is also assumed the line temperature is constant at 50 \u00b0C (122 \u00b0F). The change in pressure drop (\u0394P) due to changes in crude oil viscosity for this case study will be calculated and presented in the following sections.<\/p>\n

\"Figure
Figure 2. Measured absolute viscosity at 50\u00b0C (122 \u00b0F) for crude oils without chemical<\/figcaption><\/figure>\n
\"Figure
Figure 3. Measured absolute viscosity at 50\u00b0C (122 \u00b0F) for crude oils with chemical<\/figcaption><\/figure>\n
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Tables 2a and 2b show the calculated pressure drop for four different crude oils with varying viscosities in System International (SI) and field units (FPS – Foot, Pound and Second), respectively. The measured absolute viscosities were used to calculate pressure drops for all cases. The oil flow rate is 7,950 m3\/d (50,000 bbl\/day). Table 2 indicates that by using incorporative additives a reduction of up to 24% in pressure drop is achieved for this case study. The results in this table also indicate that the percent reduction in pressure drop (0.5% for the lightest oil) is not as high as the percent reduction in viscosity (3.7% for the lightest oil). Another observation is that the reduction in viscosity and consequently in pressure drop for light crudes oils is not as significant as for the heavy crudes.<\/p>\n

Table 2a. Pipeline pressure drop for four different crude oils without and with additive at 50 \u00b0C and oil flow rate of 7,950 m3\/d<\/p>\n

\"table2a\"<\/p>\n

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Table 2b. Pipeline pressure drop for four different crude oils without and with additive at 122 \u00b0F and oil flow rate of 50,000 bbl\/day<\/p>\n

\"table2b\"<\/p>\n

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Table 2c. Reynolds number and friction factor for the cases in Table 2 a and b<\/p>\n

\"table2c\"<\/p>\n

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Similarly, for an oil flow rate of 15,900 m3\/d (100,000 bbl\/day), Tables 3a and 3b show the calculated pressure drop for the same four crude oils with varying viscosities. Tables 3a and 3b indicate that as flow rates are increased, less reduction in pressure drop is obtainable if the flow becomes turbulent. For the case of 16.4 \u00b0API, the reduction in pressure drop is 6.6% compared to 20.7 reduction when the flow rate was of 7,950 m3\/d (50,000 bbl\/day). The calculated Reynolds number, Moody friction factors for the cases of lower and higher oil flow rates are shown in Tables 2c and 3c, respectively.<\/p>\n

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Table 3a. Pipeline pressure drop for four different crude oils without and with additive at 50 \u00b0C and oil flow rate of 15,900 m3\/d<\/p>\n

\"table3a\"<\/p>\n

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Table 3b. Pipeline pressure drop for four different crude oils without and with additives at 122 \u00b0F and oil flow rate of 100,000 bbl\/day<\/p>\n

\"table3b\"<\/p>\n

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Table 3c. Reynolds number and friction factor for the cases in Table 3 a and b<\/p>\n

\"table3c\"<\/p>\n

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In order to show the impact of chemical on pipeline capacity for the same pressure drop, let\u2019s consider the heavy crude oil with 12.7 \u00b0API. As shown in Table 2a and 2b for an oil flow rate of 7,950 m3\/d (50,000 bbl\/day) the pressure drop without chemical was 4.684 MPa (679 psia). For the same pressure drop and using the reduced viscosity due to addition of chemicals, the capacity increases to 10,472 m3\/d (65,865 bbl\/day). This is equivalent of 31% increase in pipeline capacity. Similarly, referring to Tables 3a and b for an oil flow rate of 15,900 m3\/d (100,000 bbl\/day) for the case of without chemical, the pressure drop was 9.367 MPa (1358 psia). The calculated capacity for the same pressure drop is 20943 m3\/d (131,730 bbl\/day). Again, a 31 % increase in pipeline capacity is observed.<\/p>\n

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Conclusions:<\/strong><\/p>\n

The following conclusions can be made based on this case study:<\/p>\n

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  1. The mechanisms of how drag reducing agents work are different from\u00a0incorporative chemical additives. Incorporative chemical additives reduce\u00a0viscosity.<\/li>\n
  2. Utilizing incorporate chemical additives can reduce crude oil viscosity and\u00a0consequently reduces the pipeline pressure drop significantly. For existing pipelines this means an increase in the capacity of the line and\/or reduction in pump power requirement.<\/li>\n
  3. The reduction of viscosity and pressure drop are more significant for heavier crude oils. As the oil gets lighter the effect of chemical additives is diminished. At lower temperatures the oil viscosity increases; therefore, the effect of chemical additives may become more significant for lighter crude oils, too.<\/li>\n
  4. The percent reduction in pipeline pressure drop is not always as large as the percent reduction for viscosity.<\/li>\n
  5. The incorporative chemical additives are most effective for laminar flow and\/or heavier crude oils.<\/li>\n
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    A total cost analysis based on hydraulic design and chemical additives with consideration for HSE (health, safety, and environment) should be made for effective design and operation.<\/p>\n

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    To learn more about similar cases and how to minimize operational problems, we suggest attending our G4 (Gas Conditioning and Processing)<\/a>, PF4 (Oil Production and Processing Facilities)<\/a>, PL22 (Pipeline Systems Overview)<\/a> and PL42 (Onshore Pipeline Facilities – Design, Construction and Operations)<\/a>, courses.<\/p>\n

    PetroSkills offers consulting expertise on this subject and many others. For more information about these services, visit our website at http:\/\/petroskills.com\/consulting<\/a>, or email us at consulting@PetroSkills.com<\/a>.<\/p>\n<\/div>\n<\/div>\n<\/div>\n

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    Dr. Mahmood Moshfeghian<\/em><\/p>\n

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    References:<\/strong><\/p>\n

      \n
    1. Wikipedia, http:\/\/en.wikipedia.org\/wiki\/Drag_reducing_agent, 2015<\/li>\n
    2. Halloran, M.D., \u201cTaming Crude Behavior: Understanding production\n

      Additives \u2013 Part 1\u201d, PennEnergy, Oil & Gas, September 22, 2014<\/li>\n

    3. Halloran, M.D., \u201cTaming Crude Behavior: Understanding production\n

      Additives \u2013 Part 2\u201d, PennEnergy, Oil & Gas, September 24, 2014<\/li>\n

    4. Halloran, M.D., \u201cTaming Crude Behavior: Understanding production\n

      Additives \u2013 Part 3\u201d, PennEnergy, Oil & Gas, September 26, 2014<\/li>\n

    5. Halloran, M.D., \u201cIncorporative Production Additives Lower HSE Concerns &\n

      Improve Processes\u201d, Upstream Pumping-Wellhead Technology & Services, January\/February 2015, http:\/\/upstreampumping.com\/article\/2015\/incorporative- production-additives-lower-hse-concerns-improve-processes\/<\/li>\n

    6. Oil Flux Americas, LLC, www.oilfluxamericas.com, 2015<\/li>\n<\/ol>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/li>\n<\/ol>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n<\/div>\n

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      For transportation of crude oil, the pumping power requirement varies as the crude oil viscosity changes. Increasing \u00b0API or line average temperature reduces the crude oil viscosity. The reduction of viscosity results in higher Reynolds number, lower friction factor and in effect, lower pumping power requirements. In the March 2009 tip of the month (TOTM), […]<\/p>\n","protected":false},"author":23,"featured_media":0,"comment_status":"open","ping_status":"open","sticky":false,"template":"","format":"standard","meta":{"nf_dc_page":"","_monsterinsights_skip_tracking":false,"_monsterinsights_sitenote_active":false,"_monsterinsights_sitenote_note":"","_monsterinsights_sitenote_category":0,"_jetpack_newsletter_access":"","_jetpack_dont_email_post_to_subs":false,"_jetpack_newsletter_tier_id":0,"_jetpack_memberships_contains_paywalled_content":false,"_jetpack_feature_clip_id":0,"_jetpack_memberships_contains_paid_content":false,"footnotes":"","jetpack_publicize_message":"","jetpack_publicize_feature_enabled":true,"jetpack_social_post_already_shared":true,"jetpack_social_options":{"image_generator_settings":{"template":"highway","default_image_id":0,"font":"","enabled":false},"version":2},"jetpack_post_was_ever_published":false},"categories":[3,5,6,10,4],"tags":[],"coauthors":[15],"class_list":["post-2109","post","type-post","status-publish","format-standard","hentry","category-gas-processing","category-mechanical","category-pipeline","category-process-facilities","category-refining"],"jetpack_publicize_connections":[],"jetpack_featured_media_url":"","jetpack_shortlink":"https:\/\/wp.me\/p1pQc4-y1","jetpack_sharing_enabled":true,"_links":{"self":[{"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/posts\/2109","targetHints":{"allow":["GET"]}}],"collection":[{"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/posts"}],"about":[{"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/types\/post"}],"author":[{"embeddable":true,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/users\/23"}],"replies":[{"embeddable":true,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/comments?post=2109"}],"version-history":[{"count":1,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/posts\/2109\/revisions"}],"predecessor-version":[{"id":2121,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/posts\/2109\/revisions\/2121"}],"wp:attachment":[{"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/media?parent=2109"}],"wp:term":[{"taxonomy":"category","embeddable":true,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/categories?post=2109"},{"taxonomy":"post_tag","embeddable":true,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/tags?post=2109"},{"taxonomy":"author","embeddable":true,"href":"http:\/\/www.jmcampbell.com\/tip-of-the-month\/wp-json\/wp\/v2\/coauthors?post=2109"}],"curies":[{"name":"wp","href":"https:\/\/api.w.org\/{rel}","templated":true}]}}