**Table 4.**

*Data of the molar and mass composition of desalted crude.*

#### **Figure 12.**

*Graph of the vapor-liquid state isotherm.*

Molecular masses are calculated according to the rule of additivity (38):

$$\text{MsrP} = \sum M\_i \times Y\_i \tag{38}$$

Accordingly, MsrР = 180.54; MsrC = 206.77. emas = 0.747.

The amount of steam and liquid mG phases is determined by the formulas (39), (40):

*Analytical Chemistry - Advancement, Perspectives and Applications*

$$\mathbf{mP} = \mathbf{F} \times \mathbf{emas},\tag{39}$$

**2.6 Crude distillation unit (CDU) used in Russia compared to the typical model**

**Products ton/year %**

**mass**

0.42 5.93 10.74 17.28 19.86 54.25 35.51 10.24

4938.72 69109.88 125052.05 201243.36 231212.84 631556.87 413475.76

119254.770

Based on the evaluation of the concept of the technological scheme for the construction of a technological scheme of crude distillation unit at refineries in Russia. The topping column K-1 in most cases is a simple design as shown in **Figure 13** [28], although it fractionates the crude oil into the many components like ethane, light gasoline, etc.. There are schemes in which light gasoline is displayed under the distillate in the top of the column, and heavy gasoline on the side flanks of the column. The topping column K-1 collects 50–60% of the potential of light gasoline. The residues of column K-1 are therefore the raw material of the main atmospheric column. The composition of this raw material is weighted in such a way that an excessively high feed temperature is required, permissible temperature (380°C). The singularities of the topping column K-1 operation are as follows

1. Gases (LPG) 2. Fractions 35–145 3. Fractions 145–230 4. Fractions 230–320 5. Fractions 320–350

residues) 7. Drainage water

Total 1164287.39 100 Total 1164287.39 100

*The material balance of atmospheric distillation unit with operating time 340 days by year (365 days*

The target products. (sum. fractions) 6. Associated product (Atmospheric

• The low yield of rectified gasoline (5–15% of the mass of the column load)

• Extremely high liquid loading in the heating zone of the pre-evaporation column due to the low steam load worsens the conditions for steaming light

*Possible schemes of operation with oil topping column K-1. (a) Column K-1 with back topped crude. (b) Column K-1 with heavy gasoline and back topped crude. (c) Column K-1 without back topped crude.*

makes it difficult to collect the gasoline fraction from the oil;

fractions from the residue under the action of hot jet reflux;

[1, 28]:

**Figure 13.**

**131**

**Table 6.**

*20 days)* ∙ *24 h = 8280 h.*

**Feedstocks ton/year %**

*Crude Distillation Unit (CDU)*

1,159,200 3.48

*DOI: http://dx.doi.org/10.5772/intechopen.90394*

115.92

4968

1. Oil emulsion 2. Chemical agent (demulsifiers) 3. Water processing (freshwater) 4. Water vapor

**mass**

99.56 0.00

0.01

0.43

$$\mathbf{mG} = \mathbf{F} \times (\mathbf{1} - \mathbf{emas}),\tag{40}$$

where F (feedstock) is the exiting flow from the electrostatic desalter, and entering the tube furnace.

The mass of the vapor phase = 103,104 kg/h, the mass of liquid phase = 35054.88 kg/h. The mass composition of crude oil, vapor, and liquid phase after furnace are presented in **Table 5**.

### *2.5.2 Examples of material balance of atmospheric distillation unit (ADU)*

The production capacity of the atmospheric distillation unit for processing crude oils is 1,159,200 tons/year, with an initial load of 140 kg/h. This material balance as shown in **Table 6** was made based on the physicochemical characteristics of Bonga crude oil and the typical CDU model without the K-1 oil topping column.

