Thesis: Studying about Control System of DCU Dung Quat Refinery

LIST OF Figures 2 LIST OF Tables 2 TABLE OF CONTENTS 2 Chapter 1 An overview of Dung Quat Refinery 4 1.1 Geographical location of Dung Quat Refinery 4 1.2 Natural Conditions: 5 1.3 The importance of Dung Quat Refinery 6 1.4 Technical Features 7 1.5 History of Dung Quat Refinery 8 1.6 Organization Chart of Binh Son Refinery and Petrochemical Plant 11 1.7 Raw materials for Dung Quat Refinery 12 1.8 Process Units: 13 Chapter 2 Introduction of Crude Distillation Unit (CDU) 18 2.1 Introduction of Crude Distillation Unit (Unit 011) of Dung Quat Refinery 18 2.2 Mission of Crude Distillation Unit (Unit 011) 22 2.3 Characteristics of the Crude Oil input 23 2.3.1 Bach Ho Oil 23 2.3.2 Dubai Oil 25 2.4 Product Standards 25 2.5 Description of CDU processing technology 27 2.5.1 Preheater for Crude oil input 28 2.5.2 Desalter 29 2.5.3 Heat Furnace 31 2.6 Gasoline Stabilizer Tower 32 2.7 Crude Distillation Tower 33 2.7.1 Disc Structure of Distillation Tower 33 2.7.2 Description of the distillation operator 33 Chapter 3: Studying about Control System of CDU Dung Quat 40 3.1 Temperature control system of Kerosene stream. 41 3.1.1 Control Purpoes 41 3.1.2 The variables of control 41 3.1.4 Control Strategy 43 3.2 Control System of Overhead product of distillation tower 47 3.2.1 Control Purpoes 47 3.2.2 The variables of control 47 3.2.3 Schematic model 48 3.2.4 Control Strategy 49 3.3 Control System of bottom of the distillation column 54 3.3.2 The variables of control 54 3.3.3 Schematic model 54 3.3.4 Control Strategy 55 Conclusion: 60

MINISTRY OF EDUCATION AND TRAINING HANOI UNIVERSITY OF MINING AND GEOLOGY - - Graduation Thesis Nguyen Quang Trung CTTT12210127 Thesis: Studying about Control System of DCU - Dung Quat Refinery Ha Noi, - 2017 MINISTRY OF EDUCATION AND TRAINING HANOI UNIVERSITY OF MINING AND GEOLOGY - - Graduation Thesis Nguyen Quang Trung CTTT12210127 Thesis: Studying about Control System of DCU - Dung Quat Refinery SUPERVISOR: REVIEWER: Ha Noi, 6-2017 Control System of CDU Dung Quat Refinery INTRODUCTION Phân xưởng chưng cất khí (Crude Distillation Unit) phân xưởng cửa ngõ nhà máy lọc hóa dầu Dung Quất, phân xưởng cung cấp nguồn nguyên liệu cho hầu hết phân xưởng nhà máy lọc dầu Do đó, kiến thức phân xưởng vô quan trọng cho kỹ sư công nghệ hóa dầu Sự chưng cất tiến hành thiết bị chưng cất gồm tháp chưng cất thiết bị phụ trợ khác lò gia nhiệt, thiết bị tách muối… Hầu hết tháp chưng cất dùng công nghệ lọc dầu chế biến khí tự nhiên tháp đĩa, tháp chưng cất của nhà máy lọc dầu dung quất Trong tháp chưng cất có nhiều đĩa, tương ứng với dải nhiệt độ khác lại cho sản phẩm khác phục vụ cho phân xưởng phụ trợ Vì việc điều khiển nhiệt độ đầu đầu vào dòng sản phẩm việc làm vô quan trọng Nó ảnh hưởng trực tiếp đến chất lượng sản phẩm thương mại ảnh hưởng gián tiếp đến chi phí vận hành nhà máy Do đó, đồ án tốt nghiệp: “Control system of CDU Dung Quat”, em xin tìm hiểu quy trình điều khiển đặc trưng tháp chưng cất dầu thô Nhà máy lọc hóa dầu Dung Quất Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery PREFACE I sincerely thank Dr Nguyen Van Toan who has dedicated guidance and help me Thanks to the teacher's guidance, I understood the necessary issues and completed this thesis in due time However, with the large of workload and in a limited time, so during the process of compeleted this thesis I can not avoid mistakes and shortcomings I hope all of our beloved teachers would review and help me perfect my project Once again, I would like to express my deep gratitude to Dr Nguyen Van Toan and all the teachers of Oil and Gas Faculty major in Oil refining and Petrochemistry -( Hanoi University of Mining and Geology ) have helped me during years of studying and finishing this thesis Thank you sincerely! Hanoi, 6-2017 Student Nguyen Quang Trung Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery LIST OF Figures Figure 1.1: Geographical of Dung Quat Refinery in the map Figure 1.2: Organization Chart of Binh Son refinery and Petrochemical Plant Figure 1.3: Organization Chart of BSR Figure 1.4: Table of Dung Quat Refinery’s Process Unit Figure 2.1: Crude Distillation Unit (Unit 011) of Dung Quat Refinery Figure 2.2: 3D strucuture of Crude Distillation Unit from South East Figure 2.3: 3D sstrucuture of Crude Distillation Unit from West East Figure 3.0: The P&ID diagram for the crude oil distillate control system Figure 3.1: Simple model of Kerosene thermal process Figure 3.2: The P&ID diagram of Kerosene thermal control process Figure 3.3: Block diameter for the Kerosene thermal control process Figure 3.4: Simple model of Over-head product line thermal process Figure 3.5: The P&ID diagram of Over-head product thermal control process Figure 3.6: ck diameter for Over-head product thermal control process Figure 3.7: Simple model of Bottom product line control process Figure 3.8: Block diameter for Over-head product thermal control process LIST OF Tables Table 1.1 The main Process units and Offsites of Dung Quat Refinery Table 1.2 Product’s Capacity Table 2.1: Distillation Curve and Propotion Curve of Bach Ho Crude oil Table 2.2: Distillation Curve and Propotion Curve of Dubai Crude oil Table 2.3 Product Standards Talble 2.4 Summary of heat exchangers as well as hot product lines Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery TABLE OF CONTENTS Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery Chapter - An overview of Dung Quat Refinery 1.1 Geographical location of Dung Quat Refinery Dung Quat or Binh Son oil refinery, the first oil refinery of Vietnam is located at Dung Quat Economic Zone, Quang Ngai province Which has the Northwest borders Chu Lai Airport, the West borders National Highway 1A, East and Northeastern East border the East Sea And Quang Ngai city is at the Southwest Distance from Dung Quat refinery to: - To Quang Ngai city: 25-40 km - To Da Nang city: 100 km - To Hanoi: 880 km - To Ho Chi Minh City: 870 km - 13 km to Chu Lai airport - Inland Maritime road: 30 km - International Maritime road: 190 km - Geographical coordinates: 1080.47 degrees East, 150.23 degrees North latitude Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery Figure 1.1 Geographical of Dung Quat Refinery in the map 1.2 Natural Conditions: • Topographic: - Dung Quat Economic Zone or Binh Son Refining is located in the flat terrain of Quang Ngai Province, between the coast are low mountain range and sand dunes + Highest altitude : + 20m + Medium altitude: ÷ 10m + Lowest alitude : 0.1 ÷ + 3.0m - The terrain has the shape of sloping from West to East and from South to North with an average slope of 0.4 ÷ 8% • Climate: - Dung Quat Refinery is in the South Central climate region So it has two separated season + Winter: Not so cold,the average winter temperature is 19 oC and absolute minimum temperature does not fall below than 12oC + Summer: Temperature are fairly high in about months which have the average temperature of 28oC Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery Other elements: + Sunshine: Quang Ngai Province has the avarage sunny hours of 1,800 ÷ 2,000 hours per year + Wind: Quang Ngai province has a hot dry West wind in the summer, but not as powerful as the North Central Region It has long-lasting hot season, sometimes accompanied with the strong southwest winds causes drought in the area Northeast Monsoon: Often causes gusts, whirlwinds and often causes heavy rain, while temperatures drop sharply + Average wind speed : 2.9 m / s + Maximum wind speed : 40m / s + Typhoons: Quang Ngai as well as all the other central region which are sea coastal provinces are affected by storms On average per year, storms directly affects Quang Ngai province, caused heavy rain and very strong winds of level or higher There are also three to four tornados along with heavy rain and strong winds, sometimes accompanied by sea level rise 1.3 The importance of Dung Quat Refinery Over the years the world has witnessed major fluctuations and needs in the oil and refined oil markets Unstable situation in the major oil-supplying regions and the rise in demand of Oil-supplying have helped the price of Oil and gasoline increased to the record levels Especially, In the year 2008, the world crude oil market was constantly fluctuating unnormally It was the reason pushing the crude oil price to the record of 150$/barrel, and then fell down magnificently to below 45$/barrel Fluctuations in crude oil prices have had a negative impact on many economies, leading to many consequences, affecting the growth rate of many countries, including our country Vietnam To reduce the negative impact of oil price fluctuations and ensure our national energy security, Vietnam needs to be proactive in satisfying domestic demand of oilsupplying Building refineries will create a precondition for the chemical industry to Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery develop Refined products are the main raw material for polymerization production, lubricant additives and some cosmetic products Nowaday, more than 99% of the oil exports, 50% of the imported oil products are due to Foreign transport The production and consumption of oil in the country make the domestic transporting service increase, especially the shipbuilding industry grow rapidly These are two important sectors that are capable of generating great added value and a lot of potential for development So after all, Vietnam has decided to invest in building the first oil refinery in Dung Quat Quang Ngai called Dung Quat The first Oil Refinery Dung Quat is located in Quang Ngai province, in central region of Vietnam where has the lowest economic growth in the country The refinery plant located here not directly create jobs or contribute to local budgets But with the development of infrastructure including deep-water ports, roads, electricity, telecommunication networks serving refineries (without those factories) Open policies will attract domestic and foreign investment projects in Dung Quat economic zone in particular and in the central region Dung Quat has attractive comparative advantages: located in the midst of Vietnam and the region; There is Chu Lai International Airport, deep sea port; Has a new city with a full range of high quality amenities and services; To enjoy the highest privileges in Vietnam and to apply the regime and mechanism of open management in line with international practices and adaptation to the nature of economic globalization today 1.4 Technical Features Dung Quat refinery has a designed capacity of 6.5 million tons of crude oil annually, or 140 thousand barrels per day (22×103 m3/d) The capacity would be expanded to 10 million tons per year by 2013–2014 In addition to fuels, the refinery will also produce petro-chemical products The refinery complex area comprises: • Overall Refinery Process, Utility and Offsites Facilities: about 110 ha; • Crude Tank Farm and Flare Area: about 42 ha; Nguyen Quang Trung Page 10 Figure 3.3: Block diameter for the Kerosene thermal control process 3) Analysis of applicable control strategies The flow control loop with the FIC013 controller uses the feedback control strategy The Kerosene flow value is measured and feedback on the FIC013 controller This controller will compare the measured value with the initial value to give a total flow value (A) to the kernel stages The kernel stage will perform the multiplication of the total traffic value with a scaling factor from the UIC029 controller We see here that there is an interaction between the flow control circuits and the heat control of the flow , the flow controller gives the total flow value while the heat controller gives the scaling factor between the two product lines which passes through and does not pass through the heat exchanger Assuming, if for some reason Kerosene currents go out of the tower at disc number 15 less than the required value, the UIC029 controller gives the scaling factor to the kernels stage to multiply by the total stored value (A) from the TIC013 controller to increase the opening of the UV083 valve and reduce the opening of the UV084 valve.As a result, the flow of Kerosene flow that doesn’t go through the heat exchanger will increase and Kerosene flow through the heat exchanger will be increased The greater the difference in temperature, the smaller the scale factor (B) of the UIC029 As long as there is error controling system, the flow of product through the heat exchanger is still changed 3.2 Control System of Over-head product of distillation tower 3.2.1 Control Purpoes In the distillation tower, for each range of temperatures we obtain each desired product composition Therefore, to obtain the desired Over-head product composition, we must maintain the temperature at the top of the tower at a certain value To accomplish this, we extract a portion of the Over-head product line through a heat exchanger to recover the amount of heat needed to ensure the outlet heat at the top of the tower reaches the desired value 3.2.2 The variables of control For the purpose of control is to keep the output temperature from the top of the tower reach a desired value so the control variable here is the temperature The temperature of the product line coming out of the tower is denoted as T76 The temperature of the reflux stream before and after get out of the heat exchanger is denoted as T 73, T72.Because the heat exchange here supported by air, the temperature of the inlet and outlet air is marked as Tk1, Tk2.The flow of the product line and the cooling air stream are respectively denoted as Wi and Wk In particular, the product flow which passed through and not through the heat exchanger are respectively denoted W t1 and wt2 We have: wt2 + wt1 = wt Considering the causal relationship, we can recognize that during the heat exchanger process there are variables such as T76, T72, T73, Tk2 and wt However, according to technology requirements we can immediately see the variable that needs to be controlled is T76 (product's output temperature) In addition, another variable that we need to control is the flow of the wt product line because when the flow of this product line changes, it will affect the flow temperature of the product coming out of the tower The temperature of the reflux stream before and after the T 73, T72 heat exchanger is measured and feedback for use in the control algorithm Input variables are defined as Tk1, wk, wt1, and wt2 It is easy to realize that the variable that needs to be controlled is the flow of the process flow through and not through the heat exchanger wt1, wt2 The second control variable can be the flow of cooling air flow, but controlling the flow of cooling air is difficult to achieve so we consider it is interference Within the scope of the heat exchanger, we can not interfere with the temperature of the cooling air stream so these variables are also considered interference Therefore, only the flow of the product line that passes through and does not pass through the w t1, wt2 heat exchanger is chosen as the potential control variable 3.2.3 Schematic model By distinguishing these process variables above, we can provide a simplified model for the Temperature Controlling system of Over-head product line as follows: Figure 3.4: Simple model of Over-head product line thermal process 3.2.4 Control Strategy 1) Description of the P&ID diagram The P&ID diagram describe the Overhead product thermal process is simplified as the figure below: Figure 3.5: The P&ID diagram of Over-head product thermal control process The product which comes from disc number will pass through the E1112 heat exchanger and then returned to the distillation column at disc number The top tower temperature controller is based on the temperature value measured from the top of the tower to set the required temperature value for the UIC030 controller This controller is based on the required value from the TIC076 controller, the flow of the product line exits the tower and the temperature difference between the incoming product line and the outcoming product line of the tower Allowing Over-head product line to pass through the heat exchanger more or less by properly closing or opening the UV079 and UV080 control valves through the following procedure installed in the calculation block FY096 It is calculated in the equation: When Q is the amount of heat to be recovered (MW) TD is the temperature difference between the input product line and output product line (° C) F is the product flow rate going out of the tower (kg / hr) Cp is the average specific heat (Mj / kg ° C) Any increase in flow of product coming out of the distillation tower exceeds the required value The FIC011 controller will reduce the output to close both UV079 and UV080 valves through the same value computed in calculation blocks FY095 and FY097 and the result is reducing the flow Any increase in temperature above the required value at the UIC030 controller The controller will reduce the output value to close the UV080 valve through the calculation block FY097 and simultaneously open the UV079 valve through the calculation block FY095 As a result, there will be fewer product lines go through the E1112 heat exchanger and more product lines go through the UV079 valve Therefore, the top tower temperature will decrease We have: - The value of calculation block FY095: OP= A*(1-B) - The value of calculation block FY097: OP= A*B when: OP is the value of the value algorithm A is the output value of the controller FIC011 B is the output value of the controller UIC030 2) Analysis of applicable control strategies From the simplified P&ID diagram above, we can build a block diagram as shown in Figure 3.6 below Figure 3.6: Block diameter for Over-head product thermal control process The purpose of this control loop is to maintain the temperature of the product coming out of the top of the tower at a desired temperature, thereby ensuring the quality of the overhead product line The temperature control system of overhead product line uses a floor-control structure to control the temperature of the top product line coming out of the distillation tower In it, the temperature control loop determines the quality of the top product line component However, because thermal procecss is a slow-moving process, Overhead temperature control will not achieve the desired value if we not include a fasteraction control loop Indeed, the temperature value of the T76 Overhear product is measured and feedback of the TIC076 controller, which compares the feedback value and the initial value to the set value for the Heat temperature control unit UIC030 This is a controller that has a rapid impact on the temperature change, ensuring that the temperature of the peak flows out of the tower to the desired value The heat control loop uses feedback control strategies The controller relies on signals such as the difference in the temperature of the flow of reflux before and after passing through the heat exchanger as well as the flow rate of the reflux stream to be calculated and compared to the settle value, which equired by temperature controller TIC076 Based on this deviation value, the controller will introduce a proportional factor (B) to the kernel to close the UV079 valve and open the UV080 valve and opposite also The flow control loop also uses a feedback control strategy to control the flow of product which through it, we can control the temperature of the product that comes out from the top of the tower Indeed, the flow of the reflux stream is measured and taken to the flow controller Based on the difference between the setpoint and the measured flow, the controller outputs a total flow signal (A) to the kernel to close or open two valves UV079 and UV080 We see here the interaction between the two flow control and the heat control, the flow controller gives the total flow value while the heat controller gives the scale factor between the product passes through and does not pass through the heat exchanger with the reflux flow product Assuming, for some reason, that the Overhead product line temperature goes out of the tower is smaller than the set value, the TIC076 controller will give a value corresponding to the temperature decreased to the UIC030 controller The UIC030 controller will provide a scaling factor to the calculation block FY095 to increase the opening of the UV079 valve so that the flow of product through the heat exchanger will increase At the same time, the UIC030 controller will also apply that scalling factor to the calculation block FY097 to reduce the opening of the UV080 valve The greater the difference in temperature, the smaller the scale factor (B) of the UIC030 controller As long as the deviation is controlled, the flow of product through the heat exchanger is changed Through analysis of the floor control structure above, we see that the TIC076 controller acts as a primary controller, while the UIC030 controller is a secondary controller The secondary controller receives the signal from the primary controller as its setpoint value In general, the floor control structure, internal control loops are faster than external control loops to eliminate local interfience, improve stability and system sustainability 3.3 Control System of bottom of the distillation column 3.3.1 Control Purpoes Controlling the level of the bottom of the distillation column is an absolute necessity to ensure that the amount of liquid at the bottom of the tower does not exceed an allowable value Thereby, increasing the distillation efficiency into the petroleum segments for the tower In addition, controlling the level at the bottom of the distillation tower avoids the phenomenon of "flooding" the tower, making the product of distillation process more residues, thus reducing the economic efficiency 3.3.2 The variables of control For the purpose of control here is to keep the amount of liquid at the bottom of the tower always at a certain value so the variable that needs to be controlled here is the liquid level at the bottom of the tower and is denoted h It is also easy to recognize the flow of crude oil into the tower w and the flow rate of the bottom product wb are the input variables Bottom’s products flow through the RFCC workshop and to the tank is denoted wb1, wb2, wb3 respectively We have: wb1+wb2+wb3=wb The flow into the tower w depends on the operating mode of the tower as well as the effect of distillation on the lighter segments, which we consider as interference The interference variables listed here are the temperature at the bottom of the tower as well as the temperature of the crude oil and are generally denoted by T, the flow of crude oil into the tower and the working pressure of the tower Therefore, the potential control variables are the flow of the bottom product flow to the RFCC workshop and storage tank denoted by wb1,wb2,wb3 3.3.3 Schematic model By differentiating the process variables above, we can come up with a simple model that performs the problem of temperature control of the bottom product of the tower as shown below: Figure 3.7: Schematic model of Bottom product line control process 3.3.4 Control Strategy Description of the P&ID diagram A simple P & ID diagram depicting the bottom product of the tower control process is shown as figure below: Figure 3.7: The P&ID diagram of bottom productl control process The bottom of the main distillation column T-I101 is controlled by the LIC007 level controller with three different divisions When the amount of liquid at the bottom of the tower is low about (0 - 33%), the control signal from the LIC007 controller after passing LY-082 to convert the signal from 0- 33% to 0-100% will be transmitted to the LY-007B signal selector, this selector will compare the signal from LIC007 and the signal from the 15-LIC402 level controller from the RFCC workshop to control the amount of material needed for the RFCC unit When the amount of liquid at the bottom of the tower is at an average (33-67%), the LIC007 controller will send the required reset signal to the flow controller PQIC026 and in case the amount of liquid at the bottom of the tower is high (67-100%), the LIC007 controller will send the required reset signal to the flow controller PQIC027 The two flow controllers FQIC026 and PQIC027 are parallel controllers used to regulate the flow of bottom product to the tank in case the bottom product volume is greater than 33% In the case of RFCC unit shutdown, the FQIC026 controller will signal fully open the FV026 valve and the FQIC027 controller will send a signal to control the opening of the FV027 valve thereby controlling the flow of the product line to the storage tank Block Diagram From the simplified P&ID diagram above, we can build a block diagram as shown in Figure 3.8 below: Figure 3.8: Block diameter for Over-head product thermal control process Analysis of applicable control strategies The bottom level control system uses a floor control strategy with LIC007 as the primary controller, while the flow controllers are secondary controllers The flow controllers receive value from the primary controller as the value set by themselves to directly control the aperture of the control valves to the required value As a result, the liquid level at the bottom of the tower is always maintained at a fixed band The flow control loop uses feedback control strategies to control the flow of each product flow to the RFCC Unit and to the storage tank The flow controller is used here for the purpose of maintaining the position of the control valve according to the control signal from the level controller, by comparing the control signal from the LIC007 level controller and the signal from the flow measurement device The level control loop also uses a feedback control strategy in combination with a partition control that maintains the bottom of the tower liquid at a certain value Indeed, the liquid level signal at the bottom of the tower is continuously measured by LT007 and taken to the LIC007 level controller Based on the difference between the set point and the liquid level measured at the bottom of the tower, the controller will issue control signals corresponding to each deviation to thereby control the opening of valves Assuming, for some reason, the amount of liquid at the bottom of the tower increases and is very high (67-100%), in addition to signaling the PQIC029, FỌIC026 controllers to fully open the valves FV029, FV026, LIC007 controller will also give control signal to controller FQIC027, controller FQIC027 will give signal to open valve FV027 and consequently the amount of liquid at the bottom of tower will decrease Particularly for the FQIC029 controller, in addition to receiving signals from the LIC007 controller, it also receives signals from I5-LIC402 to compare these two values And for smaller values, the control signal for the FV029 valve will be provided to ensure the bottom flow to the RFCC, which is a selective control strategy for system safety If the liquid at the bottom of the tower is in the range of 33-67%, the LIC007 controller will send the control signal to FQIC029 to fully open the FV029 valve (control of the opening of the valve FV029 depends on the control signal from 15LIC402 at the RFCC workshop) and giving the control signal to FQIC026 to change the aperture of the FV026 valve until the amount of liquid in the tower reaches the desired value At this time there is no product line through the valve FV027 3.4 Assess on structure and appicable control strategy Control system for distillation towers is a very complex system with many variables interacting with each other However, for the control system of the crude oil distillate at Dung Quat oil refinery, the control requirements not necessarily have to be given to each specific product contained in the crude oil component It just distillate into segments of crude oil And these segments will be the raw materials for the next processing units to obtain higher value products Therefore, the control loops analyzed above did not mention the effect, the interaction between the temperature variables at each tray together We are only in-depth study and analysis of control methods which is used to see this as a reference for successful, stablefor future operation of the Refinery Indeed, after studying the design documentation of the Technip contractor for the factory, especially about the control system for the crude oil distillation column, the following results were drawn: • The control system for the distillation tower still employs the most commonly used controls in the world today, using control strategies such as linear control, feedback control, scaling control , and controllers use the PiD algorithm to achieve the control purposes required by the problem • Although the control system for the tower is separated into individual control loops, it does not affect the quality of the output products Because, for individual control loops, a certain degree of interactivity has been taken into account from other control loops • However, through the analysis, I noticed that there are some disadvantages that the control system for the distillation tower needs to pay attention to That the system did not mention the quality of the products coming out of the distillation column using separators to collect data from the products, so can have more accurate control methods • While here only use a single control variable is the temperature to produce products that correspond to certain temperature ranges • For the bottom-level control problem, the conditioning system did not provide methods to compensate for the noise of the process Conclusion:  I have studied the engineering design documentation of the control system related to crude oil distillate at Dung Quat Refinery to rebuild simplìied P&ID diagrams and block diagrams  The thesis has explored the methodology for theoretical modeling of the distillation tower in general as well as exploring the applied distillation technologies nowaday  The thesis has studied the process control strategies in which the application of analytical control strategies was used for control of crude oil distillation of the Dung Quat oil refinery  The thesis also gave the author's comments on the control structure applied to the control system of crude oil distillation column at Dung Quat oil refinery  The temperature control of the main distillation column directly affects the quality of the output products, so studying about it, is really important if we want to increase the quality as well as the commercial purposes ... Refinery TABLE OF CONTENTS Nguyen Quang Trung Page Control System of CDU Dung Quat Refinery Chapter - An overview of Dung Quat Refinery 1.1 Geographical location of Dung Quat Refinery Dung Quat or Binh... Quang Trung Page Control System of CDU Dung Quat Refinery LIST OF Figures Figure 1.1: Geographical of Dung Quat Refinery in the map Figure 1.2: Organization Chart of Binh Son refinery and Petrochemical...MINISTRY OF EDUCATION AND TRAINING HANOI UNIVERSITY OF MINING AND GEOLOGY - - Graduation Thesis Nguyen Quang Trung CTTT12210127 Thesis: Studying about Control System of DCU - Dung Quat Refinery