CN109299838B

CN109299838B - Refinery process energy consumption analysis method and device

Info

Publication number: CN109299838B
Application number: CN201710604314.6A
Authority: CN
Inventors: 胡珺; 张伟; 郭土; 王红涛; 张英; 胡丞
Original assignee: China Petroleum and Chemical Corp; Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Current assignee: Sinopec Dalian Petrochemical Research Institute Co ltd; China Petroleum and Chemical Corp
Priority date: 2017-07-24
Filing date: 2017-07-24
Publication date: 2022-02-08
Anticipated expiration: 2037-07-24
Also published as: CN109299838A

Abstract

The invention provides a refinery process energy consumption analysis method and a device, wherein the method comprises the following steps: establishing an actual energy model of the residual oil hydrogenation device and verifying the actual energy consumption of the residual oil hydrogenation device according to the calibrated reference working condition data and the calibrated process data; the method comprises the steps of determining the operation condition with the lowest energy consumption which can be realized by a residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting preset quality requirements of products according to calibrated throughput and product yield without changing the existing process flow, carrying out relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device and carrying out simulated calculation on the theoretical energy consumption of the residual oil hydrogenation device; and the energy-saving potential of the residual oil hydrogenation device is excavated by comparing the difference between the actual energy consumption and the theoretical energy consumption. The method can firstly obtain the minimum energy consumption theoretically reached by the residual oil hydrogenation device, and then compares the minimum energy consumption theoretically reached with the actual energy consumption, thereby being beneficial to exploiting the energy-saving potential of the residual oil hydrogenation device.

Description

Refinery process energy consumption analysis method and device

Technical Field

The invention relates to the technical field of refinery process energy consumption calculation, in particular to a refinery process energy consumption analysis method and a refinery process energy consumption analysis device.

Background

In recent years, under the competitive pressure of the deterioration of crude oil properties, the increase of light oil demand and the stricter fuel oil and environmental protection standards, oil refiners addThe proportion of industrial heavy crude oil and high-sulfur crude oil is getting larger and larger, and the technology for producing low-sulfur and ultra-low-sulfur clean fuel is rapidly developed. The residual oil hydrogenation technology can greatly improve the yield of light oil and reduce SO_xAnd carbon emission, meets the requirements of constructing resource-saving and environment-friendly novel oil refining enterprises, and is widely concerned by the oil refining enterprises.

The residual oil hydrogenation technology is a process technology for catalytic reaction of hydrogen and residual oil under the action of high pressure, high temperature and a catalyst, wherein impurities such as metal, nitrogen, sulfur and the like in residual oil molecules respectively react with hydrogen sulfide and hydrogen to generate metal sulfide, ammonia and hydrogen sulfide. The larger molecules in the residual oil can be cracked and hydrogenated at the same time, and ideal small molecular components are generated. After hydrotreatment, the residual oil can be directly used in cracking and catalytic processes and can be converted into resources such as diesel oil, gasoline and the like.

The feeding of a residual oil hydrogenation device and the temperature rise and pressure rise of hydrogen both need to supply a large amount of energy, and in order to maintain a certain hydrogen partial pressure in the reaction process, a certain amount of circulating hydrogen needs to be maintained in the reaction process besides the input of supplementary new hydrogen with higher purity; to regulate and control the reaction temperature, it is also necessary to recycle hydrogen to supply a significant amount of quench hydrogen. The boosted pressure delivery of recycle hydrogen also requires the consumption of power from the recycle hydrogen compressor. The residual oil hydrogenation process is a strong exothermic reaction, the hydrogen consumption is large, and the quantity of heat and low-temperature heat which can be recycled are also large. Therefore, the residual oil hydrogenation device is one of devices with larger energy consumption in an oil refinery, and the residual oil hydrogenation device with reduced energy consumption is beneficial to reducing the total energy consumption of the whole plant.

The existing residual oil hydrogenation energy consumption calculation methods all adopt an empirical correlation or statistical method, and the energy consumption of a residual oil hydrogenation device cannot be accurately calculated. In addition, the energy consumption can not be calculated reasonably according to the individual conditions such as the actual process level, the processing scheme and the like of each set of device; the changes of the new raw materials and the new process cannot be completely and accurately reflected. Therefore, the minimum energy consumption theoretically achievable by the device cannot be reflected, which is detrimental to the energy saving potential of the excavating device.

Disclosure of Invention

Aiming at the defects in the prior art, the invention provides a refinery process energy consumption analysis method and a refinery process energy consumption analysis device, which can reflect the theoretically-achievable minimum energy consumption of a residual oil hydrogenation device, and further compare the theoretically-achievable minimum energy consumption with the actual energy consumption, so that the energy-saving potential of the residual oil hydrogenation device is favorably exploited.

In a first aspect, the invention provides a refinery process energy consumption analysis method, which comprises the following steps:

s1, calibrating the related data under a reference working condition, taking the calibrated data as reference working condition data, and taking the calibrated process operation parameters as basic data for establishing an actual energy model;

s2, establishing an actual energy model of the residual oil hydrogenation device by using process simulation software according to the calibrated reference working condition data and process data, and calculating one or more single energy consumptions of circulating water, deoxygenated water, power consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established actual energy model, so as to verify the actual energy consumption of the residual oil hydrogenation device;

s3, without changing the existing process flow, determining the lowest energy consumption or the best energy consumption operation condition of the residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of the product according to the calibrated throughput and the product yield, performing relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating the theoretical energy consumption of the residual oil hydrogenation device according to the established theoretical energy model;

and S4, comparing the actual energy consumption with the theoretical energy consumption, analyzing the difference of the preset parameters, and excavating the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption.

Further, the S3 includes:

the method comprises the steps of analyzing theoretical working conditions of a reaction part, a stripping tower and a fractionating tower part without changing the existing process flow, determining the lowest energy consumption or the best energy consumption operation condition of a residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of a product according to the calibrated treatment capacity and the product yield, performing relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating one or more single theoretical energy consumptions in circulating water, deoxygenated water, electricity consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model.

Further, the method, without changing the existing process flow, analyzes theoretical conditions of a reaction part, a stripping tower and a fractionating tower part, determines the lowest energy consumption or the best energy consumption operation condition of a residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting preset product quality requirements according to the calibrated throughput and product yield, performs relevant calculation regulation, establishes a theoretical energy model of the residual oil hydrogenation device by using flow simulation software, and simulates and calculates one or more single theoretical energy consumption of circulating water, electricity consumption, steam, fuel gas consumption, low-oxygen-removal, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model, and specifically comprises the following steps:

theoretical working condition analysis is carried out on the reaction part, the stripping tower part and the fractionating tower part without changing the prior process flow;

wherein, the reaction part in the theoretical working condition analysis comprises a raw material, a circulating hydrogen heat exchange process, a reaction and high-low separation part; the theoretical energy consumption of the reaction part is specifically the fuel gas consumption of the reaction heating furnace and the steam consumption of the steam turbine, and the theoretical working conditions of the reaction part are analyzed through the two parts; the fuel gas consumption of the reaction heating furnace depends on the heat exchange temperature of the raw materials, and the heat high temperature affects the final heat exchange temperature of the raw materials and the energy consumption and operation of a fractionation part;

wherein, the theoretical energy consumption of the stripper part in the theoretical working condition analysis is the lowest energy consumption under the condition of ensuring the product quality and the yield;

wherein, the theoretical energy consumption of the fractionating tower part in the theoretical working condition analysis is the lowest energy consumption under the condition of ensuring the product quality and the yield;

correspondingly, according to the established theoretical energy model, one or more single theoretical energy consumptions of circulating water, deoxygenated water, power consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency are calculated in a simulation mode, and the method specifically comprises the following steps:

calculating the theoretical medium-pressure steam consumption by combining the medium-pressure steam consumption with the steam consumption of the stripping tower and the medium-pressure steam consumption of the steam turbine under the theoretical working condition;

the low-pressure steam consumption accounts for the steam production amount through the heat amount of the process side according to the steam production point and the steam consumption point;

the steam yield is calculated by the low-pressure steam consumption through the process side heat quantity according to the steam yield point and the steam consumption point;

calculating the circulating water consumption according to the heat load at the side of the process, and calculating according to the specified temperature difference of the return water on the circulating water, the cooling water injection condition of the deoxygenation water cooler under the theoretical working condition and the change of the acid water quantity;

the amount of the deaerated water is calculated according to the steam yield and the amount of the deaerated water injected, and the steam drum is regularly and continuously discharged and is uniformly considered according to 2 percent; the deaerated water cooler is deaerated water for cooling water injection, and deaerated water is not needed for water injection under theoretical working conditions;

calculating the power consumption according to the specified values of the power consumption of the pump, the load of the air cooler and the power consumption of the unit air cooling load in the theoretical working condition;

the low-temperature heat is taken according to the low-temperature heat generated by the design of the device, and the process logistics cooling temperature under the theoretical working condition is calculated;

the heat output and the heat input of the raw oil are calculated according to the national standard GB/T50441 and 2007 petrochemical engineering design energy consumption calculation standard, and the heat output of the residual oil and the heat input of the raw oil are specified;

the fuel gas consumption is calculated and regulated according to a theoretical energy model, the exhaust gas temperature and the oxygen content of the flue gas, and the heating furnace efficiency and the total heat of the heating furnace under the theoretical exhaust gas temperature of the heating furnace are calculated by utilizing the theoretical energy consumption model, so that the fuel gas consumption of the heating furnace is calculated.

Further, the reference working condition is a working condition under a normal processing load, and when the related data is calibrated under the reference working condition, the calibration period is continuous for 72 hours.

Further, the reference condition data includes: one or more of raw materials, products, processing loads, and material balance;

wherein the material balance comprises pretreatment material balance and reforming material balance, and the data content comprises yield and 72-hour accumulated flow;

the basic data comprises oil product analysis data, gas analysis data, operating parameters, current data and calibrated public engineering consumption;

the oil analysis data comprises the density, the sulfur content, the nitrogen content, the carbon residue, ASTM D86 data and the composition condition of the raw oil, and the product density, the sulfur content and ASTM D86 data;

the gas analysis data comprises analysis data of the composition of fresh hydrogen, circulating hydrogen, low-pressure gas, dry gas before desulfurization, fuel gas and flue gas of the heating furnace;

the operating parameters include flow, temperature, pressure, volume fraction and differential pressure data of each relevant stream and equipment;

the current data comprises current data of related pumps, air coolers, compressors and fans;

the calibrated utility consumption comprises circulating water, deoxygenated water, electricity, steam input of each pressure level, steam output of each pressure level, fuel gas, low-temperature heat, heat output and raw oil heat input data.

In a second aspect, the present invention further provides an apparatus for analyzing process energy consumption of a refinery, comprising:

the data calibration module is used for calibrating the related data under the reference working condition, taking the calibrated data as the reference working condition data and taking the calibrated process operation parameters as the basic data for establishing the actual energy model;

the actual energy consumption verification module is used for establishing an actual energy model of the residual oil hydrogenation device by using flow simulation software according to the calibrated reference working condition data and process data, and calculating one or more single energy consumptions of circulating water, deoxygenated water, power consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established actual energy model so as to verify the actual energy consumption of the residual oil hydrogenation device;

the theoretical energy consumption calculation module is used for determining the lowest energy consumption or the best energy consumption operation condition of the residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of the product according to the calibrated throughput and the product yield without changing the existing process flow, carrying out relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating the theoretical energy consumption of the residual oil hydrogenation device according to the established theoretical energy model;

and the energy-saving potential mining module is used for comparing the actual energy consumption and the theoretical energy consumption, analyzing the difference of each preset parameter and mining the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption.

Further, the theoretical energy consumption calculation module is specifically configured to:

According to the technical scheme, the refinery process energy consumption analysis method and the refinery process energy consumption analysis device provided by the invention utilize the process simulation software to establish an actual energy model and account for the actual energy consumption of the device according to the calibrated treatment capacity, product yield, process and equipment operation parameters and the like of the residual oil hydrogenation device, perform theoretical working condition analysis on the process flow and the equipment under the condition of meeting the product quality requirement, adopt optimized process and equipment operation parameters to provide the lowest energy consumption or the optimal energy consumption operation condition which can be realized by the residual oil hydrogenation device, perform relevant calculation regulation, utilize the process simulation software to establish the theoretical energy model of the residual oil hydrogenation device, perform simulated calculation on the energy consumption under the ideal working condition, thereby obtaining the more accurate theoretical energy consumption of the residual oil hydrogenation which is more in line with the actual production condition of the device, namely obtaining the lowest energy consumption which can be theoretically reached by the residual oil hydrogenation device, and the theoretical lowest energy consumption can be compared with the actual energy consumption, so that the energy-saving potential of the residual oil hydrogenation device is favorably exploited.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

FIG. 1 is a flow chart of a refinery process energy consumption analysis method according to an embodiment of the present invention;

FIG. 2 is a schematic representation of the amount of stripping steam as a function of the sulfur content of the bottoms oil;

fig. 3 is a schematic structural diagram of an apparatus for analyzing refinery process energy consumption according to another embodiment of the present invention.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

An embodiment of the present invention provides a refinery process energy consumption analysis method, referring to fig. 1, the method includes the following steps:

step 101: and calibrating the related data under the reference working condition, taking the calibrated data as the reference working condition data, and taking the calibrated process operation parameters as the basic data for establishing the actual energy model.

Step 102: and according to the calibrated reference working condition data and process data, establishing an actual energy model of the residual oil hydrogenation device by using process simulation software, and calculating one or more single energy consumptions of circulating water, deoxygenated water, electricity consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established actual energy model, so as to verify the actual energy consumption of the residual oil hydrogenation device.

Step 103: the method comprises the steps of determining the lowest energy consumption or the best energy consumption operation condition of the residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of the product according to the calibrated throughput and the product yield without changing the existing process flow, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating the theoretical energy consumption of the residual oil hydrogenation device according to the established theoretical energy model.

Step 104: and comparing the actual energy consumption with the theoretical energy consumption, analyzing the difference of the preset parameters, and excavating the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption.

From the above description, it can be seen that the refinery process energy consumption analysis method provided in the embodiments of the present invention utilizes process simulation software to establish an actual energy model and account for the actual energy consumption of the device according to the treatment capacity, product yield, process and equipment operation parameters and the like calibrated by the residual oil hydrogenation device, performs theoretical condition analysis on the process flow and the equipment under the condition of meeting the product quality requirement, adopts optimized process and equipment operation parameters to provide the operating conditions of the lowest energy consumption or the best energy consumption achievable by the residual oil hydrogenation device, performs relevant calculation regulations, utilizes the process simulation software to establish the theoretical energy model of the residual oil hydrogenation device, and performs simulated calculation on the energy consumption under the ideal condition, thereby obtaining the theoretical energy consumption of the residual oil hydrogenation more accurately and more in line with the actual production condition of the device, that is, obtaining the theoretical energy consumption theoretically achievable by the residual oil hydrogenation device, and the theoretical lowest energy consumption can be compared with the actual energy consumption, so that the energy-saving potential of the residual oil hydrogenation device is favorably exploited.

In an alternative embodiment, the step 103 comprises:

In an optional embodiment, the method, without changing the existing process flow, performs theoretical condition analysis on the reaction part, the stripping tower and the fractionating tower part, determines the operating conditions of the lowest energy consumption or the best energy consumption of the residual oil hydrogenation device by using optimized process and equipment operation data under the condition of meeting preset product quality requirements according to the calibrated throughput and product yield, performs relevant calculation rules, establishes a theoretical energy model of the residual oil hydrogenation device by using flow simulation software, and simulates and calculates one or more individual theoretical energy consumptions of circulating water, deoxygenated water, electricity consumption, steam of each pressure level, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model, and specifically includes:

wherein, the theoretical energy consumption of the stripper part in the theoretical working condition analysis is the lowest energy consumption under the condition of ensuring the product quality and the yield, and the specific expression is as follows: the consumption of stripping steam is reduced as much as possible under the condition of ensuring that the sulfur content of the bottom oil of the stripping tower is qualified;

wherein, the theoretical energy consumption of the fractionating tower part in the theoretical working condition analysis is the lowest energy consumption under the condition of ensuring the product quality and the yield, and the specific expression is as follows: the feeding temperature of the fractionating tower is lowest, the reflux steam production of the middle section is increased, and the low-pressure steam stripping steam consumption at the bottom of the tower is reduced; the method specifically comprises the steps of fractionating tower feeding temperature analysis, middle section heat extraction analysis and steam stripping amount analysis;

In an alternative embodiment, the reference condition is a condition under normal processing load, and the calibration period is continuous for 72 hours when the relevant data is calibrated under the reference condition.

In an alternative embodiment, the reference condition data includes: one or more of raw materials, products, processing loads, and material balance;

In an optional implementation mode, the actual energy model established by the process simulation software specifically comprises unit models such as reaction, separation, heat exchange, compression and the like.

In addition, each single actual energy consumption comprises circulating water, deoxygenated water, electricity, steam input of each pressure grade, steam output of each pressure grade, fuel gas, low-temperature heat, heat output, raw oil heat input and the like. The circulating water amount verification comprises process stream cooling water and other cooling water. The power consumption verification comprises power consumption of a pump, air cooling, a compressor and a fan.

And the steam quantity verification of each pressure grade is calculated according to the steam balance of each pressure grade.

The power consumption of the pump, the unit and the electric heater is calculated by the formula

Wherein U is voltage in units of V; i is current, in units of A; cos α is the power factor.

Wherein the heat output and the heat input of the raw oil are calculated according to the national standard GB/T50441 and 2007 petrochemical engineering design energy consumption calculation standard, and the heat output of the residual oil and the heat input of the raw oil are specified;

calculating the heat of a process side and superheated steam according to an actual energy model, calculating the effective load of the heating furnace, calculating the furnace efficiency according to the data such as the composition of fuel gas, the oxygen content of flue gas and the like, and calculating the consumption of the fuel gas according to the effective heat load, the furnace efficiency and the heat value of the fuel gas; in particular the effective heat load/(furnace efficiency fuel gas heating value).

Wherein, the efficiency of the heating furnace can be calculated according to the smoke discharging temperature of the heating furnace and the excess oxygen content of the smoke; when the fuel is completely combusted, the content of incompletely combusted components in the combustion products is low and can not be considered, and therefore, the excess air coefficient can be expressed as:

wherein, O₂Is O in the flue gas₂Volume percent of CO₂Is CO in the flue gas₂Volume percentage content.

Then according to the book of tubular heating furnace, the ratio q of the heat content of the flue gas to the low heat value of the fuel₁And calculating the heat loss of the exhaust smoke of the heating furnace according to a relation graph with the temperature of the exhaust smoke. The furnace efficiency can be expressed as: 1-smoke exhaust heat loss-heat dissipation loss-chemical incomplete combustion heat loss-mechanical incomplete combustion heat loss, wherein the heat dissipation loss is calculated according to 3.5% estimation in a unified mode, and the chemical incomplete combustion heat loss and the mechanical incomplete combustion heat loss are ignored.

The actual energy consumption and the theoretical energy consumption value mentioned in the embodiment of the invention are unit comprehensive energy consumption values, and the calculation is carried out according to the real consumption or output quantity of each energy source or energy consumption working medium, the corresponding energy consumption coefficient and the device processing capacity. Specifically, the real object consumption or output quantity of each energy source or energy consumption working medium is multiplied by the corresponding energy consumption coefficient, then the energy consumption coefficient is divided by the device processing capacity, and the calculation results of each energy source or energy consumption working medium are added to obtain an energy consumption value with the unit of kgEO/t.

The refinery process energy consumption analysis method provided by the embodiment of the invention is suitable for different residual oil hydrogenation process types such as a fixed bed residual oil hydrogenation process, a moving bed residual oil hydrogenation process, a boiling bed residual oil hydrogenation process, a suspension bed residual oil hydrogenation process and the like. The types of equipment and energy consumption involved in the verification and calculation are different according to different residual oil hydrogenation process flows. Compared with the prior art, the refinery process energy consumption analysis method provided by the embodiment of the invention improves the existing process flow, process conditions and the like by adopting a new process, new equipment and a new method according to the properties of raw materials, the load of a device, a product scheme and the like, improves the energy utilization efficiency of the device, including the equipment efficiency, the heat recovery rate and the like, and calculates to obtain the theoretical energy consumption of the device. The energy-saving potential of the device is reflected by comparing the theoretical energy consumption with the actual energy consumption after checking, and a foundation is laid for the reconstruction and optimization of the device.

The invention will now be further described with reference to specific embodiments.

The design idea of the refinery process energy consumption analysis method provided by the embodiment of the invention is as follows: firstly, data under a calibration condition is taken as datum working condition data, including raw materials, products, processing loads, material balance and the like, and process operation parameters under calibration are taken as basic data for modeling. And then, establishing an energy model of the residual oil hydrogenation device according to the calibrated process and equipment data, calculating the individual energy consumption, and further checking the actual energy consumption of the residual oil hydrogenation device. On the basis of not changing the existing process flow, according to the treatment capacity and the product yield under calibration, under the condition of meeting the product quality requirement, the theoretical energy consumption of the residual oil hydrogenation device is obtained by adopting optimized process and equipment operation data and carrying out relevant calculation regulation and simulating and calculating the energy consumption under the ideal working condition. By comparing actual energy consumption and theoretical energy consumption, the difference of each key parameter is analyzed, the energy-saving potential of the residual oil hydrogenation device is excavated, and a foundation is laid for the transformation optimization of the residual oil hydrogenation device.

The refinery process energy consumption analysis method provided by the embodiment of the invention mainly adopts the following processing procedures: (1) determining a reference working condition: data under the calibration condition is taken as reference working condition data, including raw materials, products, processing load, material balance and the like, and process operation parameters under the calibration are taken as basic data for establishing an actual energy model. (2) Establishing an actual energy model: and establishing an actual energy model of the device by using process simulation software according to the calibrated process and equipment data, wherein the actual energy model comprises unit models such as reaction, separation, heat exchange, compression and the like. (3) And (4) actual energy consumption verification: and calculating the individual energy consumption of fuel, steam, electricity and the like according to the established actual energy model, and further verifying the actual energy consumption of the device. (4) Establishing a theoretical energy model: the method is characterized in that the existing process flow is not changed, optimized process and equipment operation data are adopted and relevant calculation regulations are carried out according to the calibrated throughput and product yield under the condition of meeting the product quality requirement through theoretical working condition analysis, and a device theoretical energy model is established by using flow simulation software. (5) Calculating theoretical energy consumption: and simulating and calculating the energy consumption under the ideal working condition according to the established theoretical energy model. (6) And comparing the actual energy consumption with the theoretical energy consumption, and analyzing the difference of each key parameter.

The refinery process energy consumption analysis method provided by the embodiment of the invention is explained in detail by a specific example as follows:

A. the residual oil hydrogenation device takes the mixed oil of vacuum residual oil and straight-run light and heavy wax oil as raw materials, and after the mixed oil is mixed with hydrogen, under the action of a catalyst, the mixed oil is subjected to catalytic hydrogenation reaction to remove impurities such as sulfur, nitrogen, metal and the like, so that the content of carbon residue is reduced, a high-quality raw material is provided for a catalytic cracking device, a part of diesel oil is produced at the same time, and a small amount of naphtha and dry gas are produced as byproducts. The device adopts a fixed bed residual oil hydrogenation process, the reaction part adopts a thermal high-resolution process flow, and the fractionation part adopts a stripping tower and a fractionating tower flow. The unstable naphtha and hydrogenated residual oil of the product are sent to a catalytic cracking device, and the naphtha and diesel oil are sent to a tank zone. And (3) taking the calibration data of the full-load working condition as a reference working condition, and simultaneously calibrating the related data under the working condition, wherein the calibration period is 72 hours in total. The baseline operating conditions data are shown in the following table:

TABLE 1 Material balance Table

Table 2 oil analysis data sheet (D86)

Item	Unit of	Mixed raw oil	Hydrogenated residual oil	Diesel oil	Naphtha (a)
						Density (20 ℃ C.)	kg/m³	974.56	930.28	877.08	783.65
Carbon residue (micro method)	％(m/m)	9.84	4.77
						Initial boiling point	℃			214.25	90.25
5％	℃	370	337.5
						10％	℃	396.6	357.25	242.75	138.25
30％	℃	479.6	424
						50％	℃		483	282	163.75
70％	℃		521
						90％	℃		517.5	320.5	193.75
95％	℃			330.5
						End point of distillation	℃	528.4	540	337.5	206
Sulfur content	％(m/m)	3.21	0.45	0.05	0.026
						Glue	％(m/m)	13.36	6.37
Asphaltenes	％(m/m)	3.07	2.08
						Saturated hydrocarbons	％(m/m)	33.89
Aromatic hydrocarbons	％(m/m)	44.42
						Viscosity (100 ℃ C.)	mm²/s	79.64

TABLE 3 gas composition analysis data sheet

Table 4 heating furnace flue gas composition analysis data table (dry basis)

Component name	Unit of	Flue gas
			Oxygen gas	v％		2
Carbon dioxide	v％	10.9
			Carbon monoxide	ppm	0
Sulfur dioxide	mg/m³	0

TABLE 5 Main operating conditions Table

For the refinery process energy consumption analysis method provided by the embodiment of the invention, the actual energy consumption of the residual oil hydrogenation device needs to be determined first, and the determination process of the actual energy consumption of the residual oil hydrogenation device will be explained in detail below.

B. And establishing an actual energy model of the device by using flow simulation software according to the calibrated process and equipment data, calculating the individual energy consumption, and further checking the actual energy consumption of the device.

(1) Medium-pressure steam: the medium-pressure steam of the device has no steam generating point, and users comprise a steam turbine and stripping steam of a stripping tower. Through accounting, the power difference between the steam turbine and the circulating hydrogen compressor is within 5%, so that the gas consumption of the steam turbine adopts a calibration value, and detailed data are shown in a table below. Wherein, the steam turbine consumes 33.4t/h of medium pressure steam, and the steam consumption of the stripping tower is 2.5t/h, which is 35.9t/h in total.

TABLE 6 steam accounting table for steam turbine

(2) Low-pressure steam: the low-pressure steam generating point of the device comprises hydrogenated residual oil steam generation and steam generation of 1.0MPa steam generated by 3.5MPa steam backpressure of a steam turbine, the steam consuming point comprises steam stripping steam of a fractionating tower, the accounting method is to account the steam generation amount through the heat at the process side, and the low-pressure steam amount sent out by the device is 29.4 t/h.

TABLE 7 Balancing table for low-pressure steam production

(3) Low-pressure steam: the hydrogenation residual oil and the low-pressure steam are produced in the middle section of the fractionating tower in a circulating manner, and the steam yield is calculated by the heat energy of the process side and is totally 11.19 t/h.

TABLE 8 Balancing table for low-pressure steam generation

(4) Deoxygenated water: the amount of the deoxygenated water is calculated according to the steam production and the amount of the water injection deoxygenated water in the calibration report, and the steam drum is uniformly and continuously arranged and considered according to 2%.

TABLE 9 accounting of deoxygenated water usage

(5) Circulating water: the circulating water consumption is calculated according to the process side heat load, the circulating water upper return water temperature difference is calculated according to 8 ℃ because the circulating water upper return water temperature difference is unknown during the calibration period, and the cooling load verification result of the device water cooler is shown as follows. The total cooling load is 1729kW, which is converted into 186.52t/h of circulating water. Then 460.2t/h of pump cooling water was added for a total of 646.72 t/h.

TABLE 10 Water cooler Cooling load accounting

TABLE 11 accounting for circulating water quantity

Item	Unit of	Using the value
			Process stream cooling water	t/h	186.52
Other cooling water	t/h	460.20
			Total up to	t/h	646.72

(6) Electricity: the power consumption of the pump, the compressor, the fan and the air cooler is 6295.07kW in total.

(7) Low-temperature heat: the low-temperature heat output at the position 3 of the device is respectively fractionation tower top gas, diesel oil and hydrogenation residual oil, but the prior device does not produce low-temperature heat because the prior four parts of low-temperature heat are excessive.

(8) Heat output: according to the national standard GB/T50441-2007 petrochemical engineering design energy consumption calculation standard, the thermal output specified temperature of the residual oil is 120 ℃, 75% of the hydrogenated residual oil is discharged by heat at 166 ℃ during calibration, 25% of the hydrogenated residual oil is discharged to a tank region at 107 ℃, and the output heat is calculated as follows.

TABLE 12 hydrogenated resid export heat determination

(9) Raw oil heat input: according to the national standard GB/T50441-2007 petrochemical engineering design energy consumption calculation standard, the heat input specified temperature of the residual oil raw material oil is 120 ℃, the heat input of the current raw material residual oil is 150 ℃, and the input heat is calculated as follows.

TABLE 13 Heat input verification of feedstock oils

Item	Unit of	Using the value
			Flow rate of mixed residual oil	t/h	229.08
Heat input temperature of residual oil	℃	150
			Temperature specified by national standard	℃	120
Output heat	kW	4360

(10) Fuel gas: the fuel gas utilization points in the device comprise a reaction heating furnace F101 and a fractionating tower feeding heating furnace F201, and the heat value of the fuel gas is calculated according to the heat value of the standard fuel gas. The process of determining the amount of fuel gas used in the furnace is described below:

1) according to the current processing load and operation parameters of the device, simulating and calculating the effective heat load;

2) calculating the efficiency of the heating furnace by combining parameters such as the composition of the flue gas and the temperature of the flue gas;

3) calculating the fuel gas consumption according to the effective heat load, the furnace efficiency and the fuel gas heat value;

TABLE 14F 101 Fuel gas usage accounting

TABLE 15F 201 Fuel gas usage accounting

TABLE 16 statistics of Fuel gas usage

Item	Unit of	Using the value
			F101 Fuel gas consumption	t/h	0.707
F201 Fuel gas consumption	t/h	0.321
			Total up to	t/h	1.028

According to the above verification results, the actual energy consumption of the device is counted, and the results are shown in the following table.

TABLE 17 actual energy consumption statistics

The key point of the refinery process energy consumption analysis method provided by the embodiment of the invention is the acquisition of the theoretical energy consumption of the residual oil hydrogenation device, and the acquisition process of the theoretical energy consumption of the residual oil hydrogenation device is explained in detail below.

C. The method comprises the steps of establishing a theoretical energy model by using process simulation software according to optimized process and equipment operation data and relevant calculation regulations under the condition of meeting product quality requirements by theoretical working condition analysis according to calibrated throughput and product yield without changing the existing process flow, and simulating and calculating energy consumption under the ideal working condition by using flow simulation software to obtain the theoretical energy consumption of the device. The theoretical working condition is analyzed as follows:

(1) reaction section

The reaction part comprises raw materials, a circulating hydrogen heat exchange process, a reaction and a high-low separation part.

The energy consumption of the reaction part is mainly in the fuel gas consumption of the reaction heating furnace and the steam consumption of the steam turbine, and the theoretical working condition of the reaction part can be analyzed through the two parts. The fuel gas consumption of the reaction heating furnace depends on the heat exchange temperature of the raw materials, and the thermal high temperature during calibration is 358 ℃ and is designed to be 360 ℃. Because the heat high-temperature separation affects the final heat exchange temperature of the raw material and the energy consumption and operation of the fractionation part, and because the temperature during calibration is almost the same as the design temperature, the theoretical working condition adopts 358 ℃.

The reaction part maintains the data during calibration, so the amount of circulating hydrogen and new hydrogen is unchanged, and the steam consumption of the steam turbine adopts the calibration working condition.

(2) Stripping tower

The theoretical energy consumption of the stripping tower accounting is the lowest energy consumption under the condition of ensuring the product quality and yield, and the method is specifically represented as follows: the amount of stripping steam is reduced as much as possible under the condition of ensuring that the sulfur content of the bottom oil of the stripping tower is qualified. The case of optimum stripping steam usage is now accounted for.

By simulation, the stripper feed temperature was 345 ℃ under theoretical conditions, at which temperature the effect of different stripping steam amounts on the sulfur content at the bottom of the column was simulated.

Referring to FIG. 2, it can be seen from FIG. 2 that when the amount of stripping steam exceeds 2t/h, the decrease of the sulfur content of the bottom oil of the stripping tower tends to be smooth, and then the amount of stripping steam is increased, and the change of the sulfur content of the bottom oil of the stripping tower is not large, so that the amount of stripping steam of the hydrogen sulfide removal stripping tower is 2t/h under the theoretical working condition.

(3) Fractionating tower

The theoretical energy consumption of the fractionating tower accounting is the lowest energy consumption under the condition of ensuring the product quality and the yield, and the theoretical energy consumption is specifically represented as follows: the feeding temperature of the fractionating tower is lowest, the reflux steam production of the middle section is increased, and the low-pressure steam stripping steam consumption at the bottom of the tower is reduced. The following analysis accounts for the conditions under which the fractionator is least energy consuming.

a) Fractionating column feed temperature analysis

Simulation analysis proves that the quality and yield of the product can be ensured even if the fractionating tower stops feeding the heating furnace. Therefore, the feeding temperature of the fractionating tower under the theoretical working condition is the bottom temperature of the stripping tower.

b) Heat analysis from middle section

Other operating conditions and product yield are unchanged, only the heat extraction quantity of middle-section reflux is changed, the middle-section reflux flow is increased, the heat extraction quantity is increased, the naphtha dry point is increased, the initial diesel oil boiling point is reduced, the dry point is unchanged, the initial residual oil boiling point is unchanged, and the heat quantity at the tower top is reduced.

c) Stripping steam analysis

Similarly, other operating conditions and product yield are unchanged, only the amount of stripping steam is changed, the stripping steam is reduced, the dry point of naphtha is increased, the initial boiling point of diesel oil is reduced, the dry point is increased, the initial boiling point of residual oil is reduced, and the heat at the top of the tower is reduced.

Because the energy consumption is reduced by increasing the heat quantity of the middle section and reducing the consumption of stripping steam, and the dry point of naphtha is increased, the relationship between the two variables needs to be balanced in order to ensure that the dry point index of the naphtha is qualified (the process index is not higher than 230 ℃). According to the following simulation results, when the reflux amount of the middle section is 140t/h and the stripping steam amount is 3t/h, the dry point of naphtha can be ensured, and the working condition of lowest energy consumption is realized.

TABLE 18 stripping steam amount analysis Table

In conclusion, the condition that stripping steam is 3t/h and middle section reflux is 140t/h is a theoretical working condition, and the corresponding energy consumption is theoretical energy consumption. At the moment, low-pressure stripping steam is consumed for 3t/h, and middle-section reflux steam production is 6.23 t/h.

(1) Medium-pressure steam: the medium-pressure steam of the device has no steam generating point, users comprise a steam turbine and stripping steam of a stripping tower, and the circulating amount of circulating hydrogen and the inlet and outlet pressure adopt actual values, so that the medium-pressure steam consumption of the steam turbine is consistent with the actual value of 33.4t/h, and the stripping steam consumption in the theoretical working condition of the stripping tower is 2t/h, and is 35.4t/h in total.

(2) Low-pressure steam: the low-pressure steam generating point of the device comprises hydrogenated residual oil steam generation, the middle section of the fractionating tower circularly generates steam, a steam turbine generates steam with the pressure of 3.5MPa steam and the back pressure of the steam turbine generates 1.0MPa steam, the steam consuming point comprises stripping steam of a stripping tower, the steam generating amount is calculated by the heat of the process side, and the low-pressure steam amount sent out by the device is 30.69 t/h.

TABLE 19 Balancing table for low-pressure steam production

(3) Low-pressure steam: the low-pressure steam generating point of the device is hydrogenated residual oil and middle-section circulation, and the steam yield is calculated by the heat quantity of the process side and is 10.18 t/h.

TABLE 20 balance table for low-low pressure steam production

(4) Deoxygenated water: the amount of the deaerated water is calculated according to the steam yield and the amount of the deaerated water injected, and the steam drum is regularly and continuously discharged and is uniformly considered according to 2 percent. The deoxygenation water cooler is used for cooling deoxygenation water for water injection, and the deoxygenation water is not used for water injection under the theoretical working condition. Through accounting, the consumption of the deoxygenated water is 14.26 t/h.

(5) Circulating water: the circulating water consumption is calculated according to the process side heat load, the circulating water upper return water temperature difference is calculated according to 8 ℃, and the cooling load verification result of the device water cooler is shown as follows. The deaerated water cooler is deaerated water for cooling water injection, and deaerated water is not needed for water injection under theoretical working conditions; due to the change of the steam stripping amount, the amount of the acidic water also changes, specifically 17t/h of water injection, 2t/h of steam stripping in the stripping tower, 3t/h of steam stripping in the fractionating tower and 22t/h in total. The total cooling load is 1547kW, which is converted into 166.86t/h of circulating water. The total amount of pump cooling water added was 627.06 t/h.

TABLE 21 Water cooler Cooling load accounting

TABLE 22 accounting for circulating water quantity

Circulating water	Unit of	Using the value
			Process stream cooling water	t/h	166.86
Other cooling water	t/h	460.20
			Total up to	t/h	627.06

(6) Electricity: when the theoretical working condition is checked, the flow rates of the pump and the compressor and the inlet and outlet pressures are not greatly different from the actual values, so the power consumption of the pump in the theoretical energy consumption is still calculated according to the actual value, the power consumption of the air cooling is calculated according to the power consumption of the unit air cooling load, namely 0.0136kW/kW, and the total power consumption is 6375.95 kW. The results are as follows:

TABLE 23 theoretical power consumption statistical table

(7) Low-temperature heat: the device is designed to have 3 hot spots for producing low-temperature heat, namely fractionating tower top gas, diesel oil and hydrogenation residual oil, under the theoretical working condition, the temperature is calculated according to the fact that process material flow is cooled to 85 ℃, wherein the temperature of the hydrogenation residual oil still has 172 ℃ after 0.5MPa steam is produced, if the low-temperature heat is produced and the energy quality is reduced, the low-temperature heat is not produced as the heat discharged to a downstream device, and the hydrogenation residual oil does not produce the low-temperature heat. Through simulation data, the theoretical output low-temperature heat is 3830kW

(8) Heat output: according to the national standard GB/T50441-2007 petrochemical engineering design energy consumption calculation standard, the heat output regulated temperature of the residual oil is 120 ℃, and the theoretical working condition is calculated according to the fact that all hydrogenation residual oil is discharged to a downstream device in a hot mode.

TABLE 24 hydrogenated residue Heat export determination

Item	Unit of	Using the value
			Flow rate of hydrogenated residual oil	t/h	199.36
Thermal output temperature of hydrogenation residue oil	℃	173.64
			Temperature specified by national standard	℃	120
Output heat	kW	6933

(9) Raw oil heat input: according to the national standard GB/T50441-2007 petrochemical engineering design energy consumption calculation standard, the heat input specified temperature of the raw material oil of the residual oil is 120 ℃, the heat input of the current raw material residual oil is 150 ℃, and the input heat is calculated as follows.

TABLE 25 Heat input verification for feedstock oils

(10) Fuel gas: by modeling accounting, under theoretical conditions, the fractionator feed furnace F201 could be shut down, so only the fuel gas consumption of the reactor was accounted for.

TABLE 26 Fuel gas dosage verification

According to the above verification results, the theoretical energy consumption of the device is counted, and the results are shown in the following table.

TABLE 27 theoretical energy consumption statistics

Numbering	Item	Dosage of	Unit of	Coefficient of energy consumption	Energy consumption, kgEO/t
						1	Circulating water	627.06	t/h	0.1	0.27
2	Deoxygenated water	14.26	t/h	9.2	0.57
						3	Electric power	6375.95	kWh	0.26	7.24
4	3.5MPag steam input	35.4	t/h	88	13.60
						5	1.0MPag steam export	30.69	t/h	76	-10.18
6	0.5MPag steam export	10.18	t/h	66	-2.93
						7	Fuel gas	0.638	t/h	950	2.65
8	Low temperature heat	3830	kW	-	-0.72
						9	Heat output	6933	kW	-	-2.60
10	Heat input of raw oil	4360	kW	-	1.64
						Total up to					9.52

D. The actual energy consumption was compared to the theoretical energy consumption as shown in the following table.

TABLE 28 comparison of actual energy consumption with theoretical energy consumption

Numbering	Item	Actual energy consumption, kgEO/t	Theoretical energy consumption, kgEO/t
				1	Circulating water	0.28	0.27
2	Deoxygenated water	0.73	0.57
				3	Electric power	7.14	7.24
4	3.5MPag steam input	13.79	13.60
				5	1.0MPag steam export	-9.75	-10.18
6	0.5MPag steam export	-3.22	-2.93
				7	Fuel gas	4.26	2.65
8	Low temperature heat	0.00	-0.72
				9	Heat output	-1.70	-2.60
10	Heat input of raw oil	1.64	1.64
				Total up to		13.17	9.52

By comparing the difference between the actual energy consumption and the theoretical energy consumption, the method can be started from the aspects of improving heat exchange between raw materials and circulating hydrogen, reducing the hydrogen-oil ratio, improving the purity of the circulating hydrogen, reducing the consumption of medium-pressure stripping steam under the condition that the sulfur content of oil products is qualified, reusing a low-temperature heat exchanger of top gas of a fractionating tower and diesel oil when low-temperature heat is insufficient or after optimization, discharging all heat to a downstream device as far as possible when conditions allow, reducing the feeding temperature of the fractionating tower under the condition that the product quality reaches the standard, reducing the smoke discharge temperature of a heating furnace, reducing the oxygen content in smoke gas and the like, reducing the energy consumption of the device, and has guiding significance for energy conservation and consumption reduction of a residual oil hydrogenation device.

Another embodiment of the present invention provides an apparatus for analyzing energy consumption of refinery processes, referring to fig. 3, the apparatus comprising: the energy-saving system comprises a data calibration module 21, an actual energy consumption verification module 22, a theoretical energy consumption calculation module 23 and an energy-saving potential mining module 24, wherein:

the data calibration module 21 is configured to calibrate related data under a reference working condition, take the calibrated data as reference working condition data, and take the calibrated process operation parameters as basic data for establishing an actual energy model;

the actual energy consumption verification module 22 is configured to establish an actual energy model of the residual oil hydrogenation device by using the process simulation software according to the calibrated reference working condition data and process data, and calculate one or more individual energy consumptions of the circulating water, the deaerated water, the electricity consumption, the steam of each pressure level, the fuel gas consumption, the low-temperature heat, the heat output, the raw oil heat input, and the heating furnace efficiency according to the established actual energy model, so as to verify the actual energy consumption of the residual oil hydrogenation device;

the theoretical energy consumption calculation module 23 is configured to determine, without changing an existing process flow, an operation condition of the lowest energy consumption or the best energy consumption that can be realized by the residual oil hydrogenation device by using optimized process and equipment operation data under the condition that preset quality requirements of a product are met according to calibrated throughput and product yield, perform relevant calculation rules, establish a theoretical energy model of the residual oil hydrogenation device by using flow simulation software, and simulate and calculate the theoretical energy consumption of the residual oil hydrogenation device according to the established theoretical energy model;

and the energy-saving potential mining module 24 is used for comparing the actual energy consumption with the theoretical energy consumption, analyzing the difference of the preset parameters, and mining the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption.

In an optional embodiment, the theoretical energy consumption calculating module 23 is specifically configured to:

The device according to the embodiments of the present invention can be used to perform the method according to the above embodiments, and the principle and technical effects are similar, and will not be described in detail here.

In the description of the present invention, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.

The above examples are only for illustrating the technical solutions of the present invention, and not for limiting the same; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.

Claims

1. A refinery process energy consumption analysis method is characterized by comprising the following steps:

s3, without changing the existing process flow, determining the lowest energy consumption or the best energy consumption operation condition of the residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of the product according to the calibrated treatment capacity and the product yield, performing relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating one or more single theoretical energy consumptions in circulating water, deoxygenated water, electricity consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model;

s4, comparing the actual energy consumption with the theoretical energy consumption, analyzing the difference of each preset parameter, and mining the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption;

the method comprises the following steps of performing theoretical working condition analysis on a reaction part, a stripping tower and a fractionating tower part without changing the existing process flow, determining the lowest energy consumption or the best energy consumption operation condition of a residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of a product according to the calibrated throughput and the product yield, performing relevant calculation regulation, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and performing simulation calculation on one or more single theoretical energy consumption in circulating water, deoxygenated water, electricity consumption, steam of each pressure grade, fuel gas consumption, low temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model, and specifically comprises the following steps of:

2. The method of claim 1, wherein the reference condition is a condition at normal processing load and the calibration period is 72 hours continuous when the related data is calibrated at the reference condition.

3. The method of claim 1, wherein the baseline condition data comprises: one or more of raw materials, products, processing loads, and material balance;

4. A refinery process energy consumption analysis device is characterized by comprising:

the theoretical energy consumption calculation module is used for determining the lowest energy consumption or the best energy consumption operation condition which can be realized by the residual oil hydrogenation device by adopting optimized process and equipment operation data under the condition of meeting the preset quality requirement of the product according to the calibrated treatment capacity and the product yield without changing the existing process flow, establishing a theoretical energy model of the residual oil hydrogenation device by utilizing flow simulation software, and simulating and calculating one or more single theoretical energy consumptions in circulating water, deoxygenated water, electricity consumption, steam of each pressure grade, fuel gas consumption, low-temperature heat, heat output, raw oil heat input and heating furnace efficiency according to the established theoretical energy model;

the energy-saving potential mining module is used for comparing actual energy consumption and theoretical energy consumption, analyzing the difference of each preset parameter and mining the energy-saving potential of the residual oil hydrogenation device according to the difference between the theoretical energy consumption and the actual energy consumption;

the theoretical energy consumption calculation module is specifically configured to:

5. The apparatus of claim 4, wherein the reference condition is a condition at normal processing load and the calibration period is 72 hours continuously when the related data is calibrated at the reference condition.

6. The apparatus of claim 4, wherein the reference operating condition data comprises: one or more of raw materials, products, processing loads, and material balance;