Method for co-producing pentane refrigerant and pentane foaming agent in same tower

Abstract

The invention provides a same-tower co-production method of a pentane refrigerant and a pentane foaming agent, which comprises the following steps: preheating a raw material from a tank field, feeding the preheated raw material into a light component removal tower, preheating a material extracted from a tower kettle, and feeding the preheated material into an olefin removal reactor; the materials are subjected to olefin removal treatment in an olefin removal reactor, the materials subjected to olefin removal enter a product tower, a tower top external recovery product is a pentane refrigerant, and a side recovery product is a pentane foaming agent; a pentane refrigerant and a pentane foaming agent are refined by the pentane refrigerant desulfurization reactor and the pentane foaming agent desulfurization reactor respectively and then enter a product tank area. According to the method, the pentane refrigerant and the pentane foaming agent can be produced in the same tower, the production process is optimized, the equipment investment is saved, meanwhile, the production conversion process of the pentane refrigerant and the pentane foaming agent does not exist, defective products in the production conversion process of the two products do not exist, and the production cost can be reduced.

Description

Technical Field

[0001] The invention belongs to the technical field of petrochemical product production, and particularly relates to a method for co-producing a pentane refrigerant and a pentane foaming agent in a same tower. Background Art

[0002] Pentane refrigerant can be used as a condensation inducer in linear low-density polyethylene plants and can also be used to liquefy refrigerants in LNG plants. Pentane foaming agent is primarily used in the production of expandable polystyrene and can also be used in the production of rigid polyurethane foam.

[0003] Pentane refrigerant and pentane foaming agent are both produced from mixed C5 as raw material, which is separated and refined. Manufacturers have two main production options for these products: one is to switch production of both products based on orders; the other is to set up a separate production tower for each product. The first option may produce some defective products during the switchover process and also places higher demands on operators. The second option, which requires dual towers, increases construction investment and energy consumption during production. Summary of the Invention

[0004] (1) Technical issues to be resolved

[0005] The present invention provides a method for co-producing a pentane refrigerant and a pentane foaming agent in the same tower, so as to solve the technical problem of how to realize the co-production in the same tower.

[0006] (2) Technical solution

[0007] In order to solve the above technical problems, the present invention proposes a method for co-producing pentane refrigerant and pentane foaming agent in a same tower, the method comprising the following steps:

[0008] S1. The raw materials from the tank area are preheated and enter the lightness removal tower, and the materials collected from the bottom of the tower are preheated and enter the deolefination reactor;

[0009] S2. The material is deolefinated in the deolefination reactor, and the material after olefin removal enters the product tower. The top product is pentane refrigerant, and the side product is pentane foaming agent.

[0010] S3. Pentane refrigerant and pentane foaming agent are refined in the pentane refrigerant desulfurization reactor and pentane foaming agent desulfurization reactor respectively and then enter the product tank area.

[0011] Furthermore, in step S1, the raw material is mixed C5.

[0012] Furthermore, in step S1, the raw materials enter the light-removal tower after passing through the preheater, the operating pressure of the light-removal tower is 0.5-0.55 MPa, the operating temperature of the top of the tower is 56-56.5°C, the operating temperature of the bottom of the tower is 109.5-110°C, and the reflux ratio is 5-16.

[0013] Furthermore, in step S1, the C4 light components at the top of the tower are collected and transported to the cracking raw material tank area.

[0014] Furthermore, in step S2, deolefination is performed by using white earth adsorption technology or hydrogenation saturation technology.

[0015] Furthermore, in step S2, when clay adsorption technology is used, the deolefination reactor is filled with activated clay, the operating temperature is 145-147° C., and the operating pressure is 1.8-2.0 MPa.

[0016] Furthermore, in step S2, when the hydrogenation saturation technology is adopted, the light hydrocarbon removal reactor is filled with a Ni-based hydrogenation catalyst, the operating temperature is 180° C., and the operating pressure is 2.87 MPa.

[0017] Furthermore, in step S2, the operating pressure of the product tower is 0.3-0.35 MPa, the operating temperature of the tower top is 60-60.5°C, the operating temperature of the side extraction is 67.1-68.5°C, and the operating temperature of the tower bottom is 105.5-107°C.

[0018] Furthermore, in step S2, the bottom of the product tower contains heavy component materials, which are collected from outside to the cracking raw material tank area.

[0019] Furthermore, in step S3, the pentane refrigerant desulfurization reactor and the pentane foaming agent desulfurization reactor use copper-based, zinc-based or a mixture of the two desulfurizers, the operating pressure is 0.8-0.85 MPa, and the operating temperature is 45-46°C.

[0020] (3) Beneficial effects

[0021] The present invention proposes a method for co-producing pentane refrigerant and pentane foaming agent in a single tower. The method includes preheating raw materials from a tank farm before entering a lightness removal tower, and preheating raw materials collected from the bottom of the tower before entering a deolefination reactor. The raw materials undergo deolefination treatment in the deolefination reactor, and the olefin-free raw materials enter a product tower. The top-collected product is pentane refrigerant, and the side-collected product is pentane foaming agent. The pentane refrigerant and pentane foaming agent are refined in a pentane refrigerant desulfurization reactor and a pentane foaming agent desulfurization reactor, respectively, before entering the product tank farm. This method allows pentane refrigerant and pentane foaming agent to be produced in the same tower, optimizing the production process and reducing equipment investment. Furthermore, there is no need to switch between pentane refrigerant and pentane foaming agent production, and no defective products are produced during the switch between the two products, thus reducing production costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a schematic diagram of the method for co-producing pentane refrigerant and pentane foaming agent in the same tower according to the present invention. DETAILED DESCRIPTION

[0023] In order to make the purpose, content and advantages of the present invention more clear, the specific implementation methods of the present invention are further described in detail below with reference to the accompanying drawings and examples.

[0024] Example 1

[0025] Combine Figure 1 Pentane refrigerant and F3 pentane foaming agent are produced using cracked light naphtha as feedstock. The feedstock composition is shown in Table 1. After being preheated in a preheater, the cracked light naphtha enters the lightness removal tower (T1). The tower top temperature is 56.2°C, the tower bottom temperature is 109.5°C, the operating pressure is 0.5 MPa, and the reflux ratio is 15. C4 from the tower top is collected and sent to the cracking feedstock tank area. The collected material from the tower bottom is preheated and then enters the deolefination reactor (R1). The deolefination reactor (R1) is filled with activated clay and operates at a temperature of 147°C and a pressure of 1.8 MPa. The material after deolefination enters the product tower (T2). The product tower (T2) has a top temperature of 60°C, a side-strip temperature of 67.1°C, a bottom temperature of 107°C, an operating pressure of 0.35 MPa, a reflux ratio of 9, and top-of-tower gas is taken to the pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is taken to the pentane refrigerant tank farm. Side-of-tower gas is taken to the pentane foaming agent desulfurization reactor (R3). After desulfurization and refining, it is taken to the pentane foaming agent tank farm. The pentane refrigerant desulfurization reactor (R2) is filled with a copper-based desulfurizer and operates at a pressure of 0.85 MPa and a temperature of 46°C. The pentane foaming agent desulfurization reactor (R3) is filled with a zinc-based desulfurizer and operates at a pressure of 0.8 MPa and a temperature of 45°C. The bottom of the tower is taken to the cracking feedstock tank farm.

[0026] Table 1 Raw material composition of Examples 1 and 2

[0027]

[0028]

[0029] Example 2

[0030] Combine Figure 1Pentane refrigerant and F4 pentane foaming agent are produced using cracked light lithosperm as feedstock. The feedstock composition is shown in Table 1. After being preheated in a preheater, the cracked light lithosperm enters the de-lightness tower (T1). The tower top temperature is 56.2°C, the tower bottom temperature is 109.5°C, the operating pressure is 0.5 MPa, and the reflux ratio is 15. The C4 from the tower top is collected and sent to the ethylene cracking feedstock tank farm. The collected material from the bottom of the tower is preheated and then enters the de-olefination reactor (R1). The de-olefination reactor (R1) is filled with activated clay and operates at a temperature of 147°C and a pressure of 1.8 MPa. After olefin removal, the material enters the product tower (T2). The product tower (T2) has a tower top temperature of 60°C, a side-cut temperature of 67.9°C, a tower bottom temperature of 107°C, an operating pressure of 0.35 MPa, and a reflux ratio of 9.5. The top of the tower is collected and sent to the pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is collected and sent to the pentane refrigerant tank farm. The pentane refrigerant desulfurization reactor (R2) is filled with a copper-based desulfurizer, with an operating pressure of 0.85 MPa and an operating temperature of 46°C; the pentane foaming agent desulfurization reactor (R3) is filled with a zinc-based desulfurizer, with an operating pressure of 0.8 MPa and an operating temperature of 45°C. The tower bottom material is collected from outside to the cracking raw material tank.

[0031] Example 3

[0032] Combine Figure 1 Pentane refrigerant and F5 pentane foaming agent are produced using reformed tops oil as feedstock. The feedstock composition is shown in Table 2. The reformed tops oil is preheated in a preheater and then enters the lightness removal tower (T1). The tower top temperature is 56°C, the tower bottom temperature is 110°C, the operating pressure is 0.55 MPa, and the reflux ratio is 5. The top C4 is collected from the tower top and sent to the ethylene cracking feedstock tank farm. The collected material from the tower bottom is preheated and then enters the deolefination reactor (R1). The deolefination reactor (R1) is filled with activated clay and operates at a temperature of 145°C and a pressure of 2.0 MPa. The material after olefin removal enters the product tower (T2). The product tower (T2) has a top temperature of 60.5°C, a side-strip temperature of 68.1°C, a bottom temperature of 105.5°C, an operating pressure of 0.3 MPa, a reflux ratio of 13, and top-of-tower gas is taken to the pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is taken to the pentane refrigerant tank farm. Side-of-tower gas is taken to the pentane foaming agent desulfurization reactor (R3). After desulfurization and refining, it is taken to the pentane foaming agent tank farm. The pentane refrigerant desulfurization reactor (R2) is loaded with a zinc-based desulfurizer and operates at a pressure of 0.80 MPa and a temperature of 45°C. The pentane foaming agent desulfurization reactor (R3) is loaded with a copper-based desulfurizer and operates at a pressure of 0.85 MPa and a temperature of 46°C. The bottom of the tower is taken to the cracking feedstock tank.

[0033] Table 2 Raw material composition of Examples 3 and 4

[0034]

[0035] Example 4

[0036] Combine Figure 1 Pentane refrigerant and F6 pentane foaming agent are produced using reformed tops oil as feedstock. The feedstock composition is shown in Table 2. The reformed tops oil is preheated in a preheater and then enters the lightness removal tower (T1). The tower top temperature is 56°C, the tower bottom temperature is 110°C, the operating pressure is 0.55 MPa, and the reflux ratio is 5. The top C4 is collected from the tower top and sent to the ethylene cracking feedstock tank farm. The collected material from the tower bottom is preheated and then enters the deolefination reactor (R1). The deolefination reactor (R1) is filled with activated clay and operates at a temperature of 145°C and a pressure of 2.0 MPa. The material after olefin removal enters the product tower (T2). The product tower (T2) has a top temperature of 60.5°C, a side-strip temperature of 68.3°C, a bottom temperature of 105.5°C, an operating pressure of 0.35 MPa, a reflux ratio of 12, and top-of-tower gas is taken to the pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is taken to the pentane refrigerant tank farm. Side-of-tower gas is taken to the pentane foaming agent desulfurization reactor (R3). After desulfurization and refining, it is taken to the pentane foaming agent tank farm. The pentane refrigerant desulfurization reactor (R2) is loaded with a zinc-based desulfurizer and operates at a pressure of 0.80 MPa and a temperature of 45°C. The pentane foaming agent desulfurization reactor (R3) is loaded with a copper-based desulfurizer and operates at a pressure of 0.85 MPa and a temperature of 46°C. The bottom of the tower is taken to the cracking feedstock tank.

[0037] Example 5

[0038] Combine Figure 1 Pentane refrigerant and F5 pentane foaming agent are produced using raffinate C5 as feedstock. The feedstock composition is shown in Table 3. The raffinate C5 is preheated in a preheater and then fed into a lightness removal tower (T1). The tower top temperature is 56.5°C, the tower bottom temperature is 109.5°C, the operating pressure is 0.5 MPa, and the reflux ratio is 16. The tower top C4 is collected and sent to the ethylene cracking feedstock tank farm. The collected material from the tower bottom is preheated and then fed into a deolefination reactor equipped with a Ni-based catalyst. After olefin removal, the material enters the product tower (T2). The product tower (T2) has a tower top temperature of 60°C, a side-draw temperature of 68.2°C, a tower bottom temperature of 105.5°C, an operating pressure of 0.3 MPa, and a reflux ratio of 8. The tower top is collected and sent to a pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is collected and sent to a pentane refrigerant tank farm. The side-draw is collected and sent to a pentane foaming agent desulfurization reactor (R3). The pentane refrigerant desulfurization reactor (R2) is filled with zinc-based desulfurizer, with an operating pressure of 0.80 MPa and an operating temperature of 45°C; the pentane foaming agent desulfurization reactor (R3) is filled with copper-based desulfurizer, with an operating pressure of 0.85 MPa and an operating temperature of 46°C. The tower bottom material is collected from outside to the cracking raw material tank.

[0039] Table 3 Raw material composition of Examples 5 and 6

[0040]

[0041] Example 6

[0042] Combine Figure 1 Pentane refrigerant and F6 pentane foaming agent are produced using raffinate C5 as feedstock. The feedstock composition is shown in Table 3. The raffinate C5 is preheated in a preheater and then fed into a lightness removal tower (T1). The tower top temperature is 56.5°C, the tower bottom temperature is 109.5°C, the operating pressure is 0.5 MPa, and the reflux ratio is 16. The tower top C4 is collected and sent to the ethylene cracking feedstock tank farm. The collected material from the tower bottom is preheated and then fed into a deolefination reactor equipped with a Ni-based catalyst. After olefin removal, the material enters the product tower (T2). The product tower (T2) has a tower top temperature of 60°C, a side-draw temperature of 68.5°C, a tower bottom temperature of 105.5°C, an operating pressure of 0.3 MPa, and a reflux ratio of 7. The tower top is collected and sent to a pentane refrigerant desulfurization reactor (R2). After desulfurization and refining, it is collected and sent to a pentane refrigerant tank farm. The side-draw is collected and sent to a pentane foaming agent desulfurization reactor (R3). The pentane refrigerant desulfurization reactor (R2) is filled with zinc-based desulfurizer, with an operating pressure of 0.80 MPa and an operating temperature of 45°C; the pentane foaming agent desulfurization reactor (R3) is filled with copper-based desulfurizer, with an operating pressure of 0.85 MPa and an operating temperature of 46°C. The tower bottom material is collected from outside to the cracking raw material tank.

[0043] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the technical principles of the present invention. These improvements and modifications should also be regarded as the scope of protection of the present invention.

Claims

1. A method for co-producing pentane refrigerant and pentane foaming agent in the same tower, characterized in that: The same-tower co-production method comprises the following steps: S1. The raw materials from the tank area are preheated and enter the lightness removal tower, and the materials collected from the bottom of the tower are preheated and enter the deolefination reactor; S2. The material is deolefinated in the deolefination reactor, and the material after olefin removal enters the product tower. The top product is pentane refrigerant, and the side product is pentane foaming agent. S3. Pentane refrigerant and pentane foaming agent are refined in the pentane refrigerant desulfurization reactor and pentane foaming agent desulfurization reactor respectively and then enter the product tank area.

2. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, wherein: In step S1, the raw material is mixed C5.

3. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, wherein: In step S1, the raw materials enter the light-removal tower after passing through the preheater. The operating pressure of the light-removal tower is 0.5-0.55 MPa, the operating temperature of the top of the tower is 56-56.5°C, the operating temperature of the bottom of the tower is 109.5-110°C, and the reflux ratio is 5-16.

4. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, wherein: In step S1, the C4 light components at the top of the tower are collected and sent to the cracking raw material tank area.

5. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, wherein: In step S2, deolefination is carried out by using white earth adsorption technology or hydrogenation saturation technology.

6. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 5, characterized in that: In step S2, when the clay adsorption technology is used, the deolefination reactor is filled with activated clay, the operating temperature is 145-147° C., and the operating pressure is 1.8-2.0 MPa.

7. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 5, characterized in that: In step S2, when the hydrogenation saturation technology is adopted, the light hydrocarbon removal reactor is filled with a Ni-based hydrogenation catalyst, the operating temperature is 180° C., and the operating pressure is 2.87 MPa.

8. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, characterized in that: In step S2, the operating pressure of the product tower is 0.3-0.35 MPa, the operating temperature of the tower top is 60-60.5°C, the operating temperature of the side extraction is 67.1-68.5°C, and the operating temperature of the tower bottom is 105.5-107°C.

9. The method for co-producing pentane refrigerant and pentane foaming agent in the same tower as claimed in claim 1, characterized in that: In step S2, the bottom of the product tower contains heavy component materials, which are taken out to the cracking raw material tank area.

10. The method for co-producing pentane refrigerant and pentane foaming agent in the same column according to claim 1, characterized in that: In step S3, the pentane refrigerant desulfurization reactor and the pentane foaming agent desulfurization reactor use copper-based, zinc-based or a mixture of the two desulfurizers, the operating pressure is 0.8-0.85 MPa, and the operating temperature is 45-46°C.

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