Oxidation and polymerization reduction system for producing fibers

Abstract

The utility model discloses an oxidation polymerization reduction system for producing fibers, which relates to the technical field of viscose staple fiber production equipment in the textile industry and comprises a dipping barrel I, a presser, a spiral mixer, a medium-concentration slurry-porridge mixing barrel and an oxygen-alkali reaction kettle, the dipping barrel I is connected with an alkali liquor supply pipeline and is connected with an inlet of the presser through a pipeline I, and the spiral mixer is connected with an outlet of the presser through a pipeline II; a material outlet of the squeezer is communicated with an inlet of the spiral mixer, an outlet of the spiral mixer is communicated with the medium-thick slurry and porridge mixing barrel, the thick slurry and porridge mixer is connected with the oxygen-alkali reaction kettle through a pipeline II, a steam pipeline and an oxygen pipeline are arranged on the pipeline II, the spiral mixer is connected with an alkali liquor supply pipeline, and the steam pipeline is connected with a steam supply pipeline. The problems that in the prior art, in the aging drum polymerization reduction process, the occupied area of equipment is large, the standing time of cellulose in an aging drum is long, and the oxidation polymerization reduction loss is large after cellulose polymerization reduction are solved.

Description

Technical Field

[0001] This utility model relates to the technical field of viscose staple fiber production equipment in the textile industry, specifically to an oxidation depolymerization system for fiber production. Background Technology

[0002] Currently, the viscose staple fiber market is highly competitive, and the impact of energy, environmental protection, and safety factors makes survival even more challenging for related companies. In this fiercely competitive environment, it is crucial to increase market share while simultaneously improving product quality and reducing production costs, all while meeting environmental and safety production requirements.

[0003] In the production of cellulose fibers, the traditional aging process for viscose staple fibers generally employs an aging drum depolymerization process. The aging drum depolymerization process is a relatively mature piece of equipment used for viscose staple fiber production. It is approximately 26.5m long and 3m in diameter. The aging drum has rotating structures at both ends and a support roller in the middle connected to a reducer and motor to achieve rotation. The aging drum is equipped with a jacket, which can be filled with media of different temperatures (clean water, brine, etc.). By adjusting the temperature of the media in the aging drum jacket, the temperature of the alkali cellulose inside the drum can be controlled, thereby achieving the desired degree of cellulose polymerization.

[0004] This polymerization reduction method has the following drawbacks:

[0005] 1. The old-style drum equipment is relatively large in size and occupies a large area;

[0006] 2. During the production process, cellulose stays in the aging drum for a long time, and after cellulose depolymerization, the loss due to oxidative depolymerization is relatively large. Utility Model Content

[0007] This invention aims to solve the problems of large equipment footprint, long residence time of cellulose in the aging drum, and significant oxidative depolymerization loss of cellulose in the existing aging drum depolymerization process.

[0008] To achieve the above-mentioned objectives, the technical solution of this utility model is as follows:

[0009] An oxidative depolymerization system for fiber production includes an impregnation tank I, a press, a screw mixer, a medium-concentration slurry mixing tank, and an oxygen-alkali reactor. The impregnation tank I is connected to an alkali supply pipeline. The impregnation tank I is connected to the inlet of the press via pipe I. The material outlet of the press is connected to the inlet of the screw mixer. The outlet of the screw mixer is connected to the medium-concentration slurry mixing tank. The medium-concentration slurry mixing tank is connected to the oxygen-alkali reactor via pipe II. Pipe II is equipped with a steam pipe and an oxygen pipe.

[0010] The spiral mixer is connected to an alkali supply line, the steam pipeline is connected to a steam supply line, and the oxygen pipeline is connected to an oxygen supply line.

[0011] Furthermore, the material outlet end of the press is equipped with a crushing mechanism.

[0012] Furthermore, the spiral mixer is a pipeline spiral mixer, which is equipped with multiple alkali inlets and is connected to an alkali supply pipeline through the alkali inlets.

[0013] Furthermore, the medium-concentration porridge mixing tank is a vertical mixer, with an inlet I at the top and an outlet I at the bottom. The medium-concentration porridge mixing tank is equipped with a stirring mechanism with 4 to 8 layers of spiral stirring blades.

[0014] Furthermore, the spiral mixer and the medium-concentration porridge mixing tank are integrated into one unit, with the discharge end of the spiral mixer connected to the feed end of the medium-concentration porridge mixing tank.

[0015] Furthermore, the steam pipe is located near the medium-concentration porridge mixing tank; the oxygen pipe is located at the rear end of the steam pipe.

[0016] Furthermore, the steam pipeline is equipped with multiple steam inlets, and the steam pipeline is connected to the steam supply pipeline through the steam inlets.

[0017] Furthermore, a porridge pump is installed at the bottom of the medium-concentration porridge mixing tank.

[0018] Furthermore, the discharge end of the oxygen-alkali reactor is connected to the impregnation tank II via pipe III, and the impregnation tank II is connected to the alkali supply pipeline.

[0019] The beneficial effects of this utility model are:

[0020] I. This utility model proposes a novel oxidative depolymerization system for fiber production, replacing the traditional aging drum equipment for depolymerization treatment of cellulose. The working principle of this oxidative depolymerization system is as follows: by mixing oxygen, alkali solution, and cellulose in a three-phase mixture and controlling the pressure, time, and temperature conditions, the degree of polymerization of cellulose is reduced within an oxygen-alkali reactor. This replaces the traditional aging drum for reducing the degree of polymerization of alkali-treated cellulose, reducing alkali-treated cellulose loss during production, lowering production costs, and solving the technical problems of large footprint and high energy consumption associated with traditional aging processes.

[0021] II. In this utility model, the material outlet end of the press is equipped with a crushing mechanism for crushing the alkali cellulose filter cake obtained after processing by the press. The crushing mechanism is preferably designed as a multi-stage crushing structure.

[0022] Thirdly, in this utility model, the spiral mixer is a pipeline-type spiral mixer. The pipeline-type spiral mixer facilitates the thorough mixing of solid materials such as alkali cellulose with the alkali solution. It also allows for easy adjustment of the overall length of the pipeline-type spiral mixer to adapt to the production of different types of fibers. The spiral mixer is equipped with multiple alkali inlets, which are connected to alkali supply pipelines. Alkali solution can be added in stages, avoiding instability in product quality caused by adding alkali solution all at once.

[0023] IV. In this utility model, the medium-concentration porridge mixing tank is a vertical mixer. The medium-concentration porridge mixing tank has a hollow stainless steel structure. The upper end of the medium-concentration porridge mixing tank is provided with a feed inlet I; the lower end is provided with a discharge outlet I. The medium-concentration porridge mixing tank is provided with a stirring mechanism with 4 to 8 layers of spiral stirring blades to achieve further mixing of the porridge.

[0024] Fifth, this utility model also proposes a preferred integrated structure for the spiral mixer and the medium-concentration porridge mixing tank, with the discharge end of the spiral mixer connected to the feed end of the medium-concentration porridge mixing tank, ensuring continuous operation of the two sections and achieving the expected porridge mixing effect. At the same time, it can reduce the area occupied by the equipment and avoid the waste of alkali solution.

[0025] VI. In this utility model, the steam pipe is provided with multiple steam inlets, and the steam pipe is connected to the steam supply pipeline through the steam inlets. The steam supply pipeline evenly introduces steam into the steam pipe through the multiple steam inlets, so as to avoid the problem of uneven heating of the fibers causing poor quality of finished products.

[0026] VII. In this utility model, a porridge pump is provided at the bottom of the medium-concentration porridge mixing tank, and the other end of the porridge pump is connected to the oxygen-alkali reaction vessel. The porridge pump is preferably a pump with a double-headed symmetrical spiral structure, which can stir and transport the porridge through high-speed rotation.

[0027] 8. In this utility model, the discharge end of the oxygen-alkali reaction vessel is connected to the impregnation tank II through pipe III. The impregnation tank II is connected to the alkali supply pipeline. The impregnation tank II is used to dissolve the organic or inorganic impurities generated after the oxygen-alkali reaction of cellulose in the alkali solution, thereby improving the quality of cellulose and enhancing the quality of alkali cellulose preparation. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of the oxidative degradation system.

[0029] Figure 2 This is a schematic diagram of another implementation of the oxidative degradation system.

[0030] Figure 3 This is a schematic diagram of another implementation of the oxidative degradation system.

[0031] Figure 4This is a schematic diagram of another preferred embodiment of the oxidative degradation system.

[0032] Figure 5 This is a schematic diagram of another preferred implementation of the oxidative degradation system.

[0033] The components are as follows: 1. Impregnation tank I; 2. Press; 3. Spiral mixer; 4. Medium-concentration slurry mixing tank; 5. Oxy-alkali reaction vessel; 6. Alkali supply pipeline; 7. Pipeline I; 8. Pipeline II; 9. Steam pipeline; 10. Steam supply pipeline; 11. Oxygen pipeline; 12. Oxygen supply pipeline; 13. Crushing mechanism; 14. Alkali inlet; 15. Stirring mechanism; 16. Steam inlet; 17. Slurry pump; 18. Pipeline III; 19. Impregnation tank II; 20. Alkali station; 21. Steam station; 22. Oxygen station; 4.1. Feed inlet I; 4.2. Discharge outlet I. Detailed Implementation

[0034] The present invention will be further described in detail below with reference to the embodiments, but the implementation of the present invention is not limited thereto.

[0035] Example 1

[0036] An oxidative depolymerization system for fiber production relates to the technical field of viscose staple fiber production equipment in the textile industry. (Reference) Figure 1 The system includes an impregnation tank I1, a press 2, a screw mixer 3, a medium-concentration slurry mixing tank 4, and an oxygen-alkali reactor 5. The impregnation tank I1 is connected to an alkali supply pipeline 6. The impregnation tank I1 is connected to the inlet of the press 2 via pipeline I7. The material outlet of the press 2 is connected to the inlet of the screw mixer 3. The outlet of the screw mixer 3 is connected to the medium-concentration slurry mixing tank 4. The medium-concentration slurry mixing tank is connected to the oxygen-alkali reactor 5 via pipeline II8. Pipeline II8 is equipped with a steam pipeline 9 and an oxygen pipeline 11.

[0037] The spiral mixer 3 is connected to the alkali supply line 6, the steam line 9 is connected to the steam supply line 10, and the oxygen line 11 is connected to the oxygen supply line 12.

[0038] In this oxidative depolymerization system, pulp raw materials and alkali solution are added to impregnation tank I1, and after stirring, a pulp porridge is formed. After generating alkali cellulose, it is conveyed to press 2 for pulp and alkali separation. The alkali solution is recycled into the large-scale production system, while the alkali cellulose enters spiral mixer 3. Spiral mixer 3 is connected to alkali supply line 6. Through spiral mixer 3, alkali and alkali cellulose are sheared and mixed to form a pulp porridge with a concentration of 0-15%, which then enters medium-concentration pulp porridge mixing tank 4. Medium-concentration pulp porridge mixing tank 4 is a hollow stainless steel structure. The pulp porridge in medium-concentration pulp porridge mixing tank 4 is conveyed to oxygen-alkali reaction vessel 5 via a transfer pump and pipeline II8. Pipeline II8 is equipped with steam pipeline 9 and oxygen pipeline 11, which can simultaneously supply steam and high-concentration gaseous oxygen to the two pipelines respectively. Steam is introduced into steam pipeline 9 through steam supply line 10 to raise the temperature of the pulp porridge, and oxygen is introduced into oxygen pipeline 11 through oxygen supply line 12 to provide the necessary oxygen supply for the cellulose depolymerization reaction, facilitating its participation in the chemical reaction.

[0039] Finally, the porridge enters the oxygen-alkali reaction vessel 5, which is equipped with a multi-layer stirring mechanism 15 to mix the steam, oxygen, and porridge, and carry out the oxygen-alkali reaction from bottom to top.

[0040] Example 2

[0041] This embodiment is a further optimization based on Embodiment 1. The difference is that the material outlet end of the press 2 is equipped with a crushing mechanism 13. (Refer to...) Figure 2 .

[0042] In actual production, a multi-stage crushing structure can be designed according to the site conditions to improve efficiency while meeting production needs.

[0043] Example 3

[0044] The difference between this embodiment and embodiments 1-2 is that the spiral mixer 3 is a pipeline spiral mixer 3, as shown in the reference. Figure 2 The spiral mixer 3 is equipped with multiple alkali inlets 14, and the spiral mixer 3 is connected to the alkali supply pipeline 6 through the alkali inlets 14.

[0045] In this embodiment, alkali solution can be added to the alkali cellulose in stages through a spiral mixer 3 equipped with multiple alkali inlets 14, thereby achieving a thorough mixing effect and avoiding the problem of uneven product quality caused by excessive local alkali solution.

[0046] Example 4

[0047] The difference between this embodiment and embodiments 1-3 is that the medium-thickness porridge mixing tank 4 is a vertical mixer. (Refer to...) Figure 3The upper end of the medium-concentration porridge mixing tank 4 is provided with a feed inlet I 4.1; the lower end is provided with a discharge outlet I 4.2. The medium-concentration porridge mixing tank 4 is provided with a stirring mechanism 15 with 4 to 8 layers of spiral stirring blades.

[0048] Example 5

[0049] Compared with Examples 1-4, the difference in this embodiment is that the spiral mixer 3 and the medium-concentration porridge mixing tank 4 are an integral structure, and the discharge end of the spiral mixer 3 is connected to the inlet end of the medium-concentration porridge mixing tank 4. (Refer to...) Figure 4 The integrated structure occupies a relatively small area. This integrated structure can adjust the slurry concentration by controlling the flow rate of alkali solution, and also has the function of fully mixing alkali solution and cellulose. The spiral blades also realize the material conveying function.

[0050] Example 6

[0051] Compared with Examples 1-5, the difference in this embodiment is that the steam pipe 9 is closer to the medium-concentration porridge mixing tank 4; the oxygen pipe 11 is located at the rear end of the steam pipe 9, as shown in the reference. Figure 4 .

[0052] Example 7

[0053] Compared with embodiments 1-6, the difference in this embodiment is that the steam pipe 9 is provided with multiple steam inlets 16, as shown in the reference. Figure 4 Steam pipe 9 is connected to steam supply pipe 10 via steam inlet 16. In this embodiment, steam is supplied to the slurry in steam pipe 9 in sections to ensure uniform material temperature and avoid localized overheating, which could affect the quality of the final product.

[0054] Example 8

[0055] Compared with Examples 1-7, the difference in this embodiment is that the bottom of the medium-concentration porridge mixing tank 4 is equipped with a porridge pump 17. (Refer to...) Figure 4 .

[0056] Example 9

[0057] Compared with Examples 1-8, the difference in this embodiment is that the discharge end of the oxygen-alkali reaction vessel 5 is connected to the impregnation tank II 19 via pipe III 18, and the impregnation tank II 19 is connected to the alkali supply pipeline 6. (Refer to...) Figure 4 Organic or inorganic impurities generated after cellulose passes through oxygen-alkali reactor 5 dissolve in the alkali solution, and the alkali solution and cellulose are separated by press 2, thereby improving the quality of cellulose and enhancing the quality of alkali cellulose preparation.

[0058] Example 10

[0059] To facilitate public understanding of this solution, this embodiment uses a superior oxidative depolymerization system for fiber production as an example, and further illustrates the solution with reference to the illustrations.

[0060] refer to Figure 5 The oxidation and depolymerization system includes an impregnation tank I1, a press 2, a screw mixer 3, a medium-concentration slurry mixing tank 4, and an oxygen-alkali reactor 5. The impregnation tank I1 is connected to an alkali supply pipeline 6. The impregnation tank I1 is connected to the inlet of the press 2 via pipeline I7. The material outlet of the press 2 is connected to the inlet of the screw mixer 3. The outlet of the screw mixer 3 is connected to the medium-concentration slurry mixing tank 4. The medium-concentration slurry mixing tank 4 is connected to the oxygen-alkali reactor 5 via pipeline II8. Pipeline II8 is equipped with a steam pipeline 9 and an oxygen pipeline 11.

[0061] The spiral mixer 3 is connected to the alkali supply line 6, the steam line 9 is connected to the steam supply line 10, and the oxygen line 11 is connected to the oxygen supply line 12.

[0062] In this embodiment, the material outlet end of the press 2 is provided with a crushing mechanism 13.

[0063] In this embodiment, the spiral mixer 3 is a pipeline spiral mixer 3, and the spiral mixer 3 is provided with multiple alkali inlets 14. The spiral mixer 3 is connected to the alkali supply pipeline 6 through the alkali inlets 14.

[0064] In this embodiment, the medium-concentration porridge mixing tank 4 is a vertical mixer. The upper end of the medium-concentration porridge mixing tank 4 is provided with a feed inlet I 4.1; the lower end is provided with a discharge outlet I 4.2. The medium-concentration porridge mixing tank 4 is provided with a stirring mechanism 15 with 4 to 6 layers of spiral stirring blades.

[0065] In this embodiment, the spiral mixer 3 and the medium-concentration porridge mixing tank 4 are an integral structure, and the discharge end of the spiral mixer 3 is connected to the feed end of the medium-concentration porridge mixing tank 4.

[0066] In this embodiment, the steam pipe 9 is located near the medium-concentration porridge mixing tank 4; the oxygen pipe 11 is located at the rear end of the steam pipe 9.

[0067] In this embodiment, the steam pipe 9 is provided with multiple steam inlets 16, and the steam pipe 9 is connected to the steam supply pipeline 10 through the steam inlets 16. In practical applications, a stirring mechanism biased towards discharging materials can also be provided in the oxygen-alkali reaction vessel 5 as needed.

[0068] In this embodiment, the bottom of the medium-concentration porridge mixing tank 4 is equipped with a porridge pump 17.

[0069] In this embodiment, the discharge end of the oxygen-alkali reaction vessel 5 is connected to the impregnation tank II 19 via pipe III 18, and the impregnation tank II 19 is connected to the alkali supply pipeline 6.

[0070] In this embodiment, reference Figure 5The alkali solution comes from alkali station 20, the steam from steam station 21, and the oxygen from oxygen station 22. The pulp raw material and alkali solution are added to impregnation tank I1, and after stirring, a pulp porridge is formed. After generating alkali cellulose, it is pumped to press 2 for pulp and alkali separation. The alkali solution is recycled into the main production system, while the alkali cellulose is crushed by crushing mechanism 13 and then enters spiral mixer 3. Spiral mixer 3 is equipped with multiple alkali inlets 14, which are connected to alkali supply pipeline 6. The alkali supply pipeline 6 can be equipped with flow meters and solenoid valves for controllable alkali input. After the alkali and alkali cellulose are sheared and mixed by spiral mixer 3, a pulp porridge with a concentration of 0-15% is formed and enters medium-concentration pulp mixing tank 4. The medium-concentration porridge mixing tank 4 is a hollow stainless steel structure. A porridge pump 17 is installed at the bottom of the medium-concentration porridge mixing tank 4. The porridge pump 17 is a pump with a double-headed spiral structure inside. It generates self-suction and shear force through high-speed rotation. The self-suction force pushes the porridge to the next process, while the shear force can effectively mix the porridge and ensure uniformity.

[0071] In this embodiment, the spiral mixer 3 and the medium-concentration porridge mixing tank 4 are integrated into one unit. The discharge end of the spiral mixer 3 is connected to the feed end of the medium-concentration porridge mixing tank 4. The structure is ingenious and occupies a small area.

[0072] The slurry is pumped to the oxygen-alkali reactor 5 via slurry pump 17. Slurry pump 17 and oxygen-alkali reactor 5 are connected by pipe II 8. A steam pipe 9 and an oxygen pipe 11 are installed between the two pipes, allowing steam and highly concentrated gaseous oxygen to be supplied to both pipes simultaneously. Steam is supplied to steam pipe 9 via steam supply pipe 10 to heat the slurry, while oxygen is supplied to oxygen pipe 11 via oxygen supply pipe 12 to provide the necessary oxygen supply for the cellulose depolymerization reaction, facilitating its participation in the chemical reaction.

[0073] Finally, the porridge enters the oxygen-alkali reaction vessel 5, which is equipped with a multi-layer stirring mechanism 15 to mix the steam, oxygen, and porridge, and carry out the oxygen-alkali reaction from bottom to top.

Claims

1. An oxidative depolymerization system for producing fibers, characterized in that: The apparatus includes an impregnation tank I (1), a press (2), a screw mixer (3), a medium-concentration slurry mixing tank (4), and an oxygen-alkali reactor (5). The impregnation tank I (1) is connected to an alkali supply pipeline (6). The impregnation tank I (1) is connected to the inlet of the press (2) through a pipe I (7). The material outlet of the press (2) is connected to the inlet of the screw mixer (3). The outlet of the screw mixer (3) is connected to the medium-concentration slurry mixing tank (4). The slurry mixer is connected to the oxygen-alkali reactor (5) through a pipe II (8). A steam pipe (9) and an oxygen pipe (11) are provided on the pipe II (8). The spiral mixer (3) is connected to the alkali supply line (6), the steam pipe (9) is connected to the steam supply line (10), and the oxygen pipe (11) is connected to the oxygen supply line (12).

2. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The press (2) is equipped with a crushing mechanism (13) at the material outlet end.

3. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The spiral mixer (3) is a pipeline spiral mixer. The spiral mixer (3) is provided with multiple alkali inlets (14). The spiral mixer (3) is connected to the alkali supply pipeline (6) through the alkali inlets (14).

4. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The medium-concentration porridge mixing tank (4) is a vertical mixer. The upper end of the medium-concentration porridge mixing tank (4) is provided with a feed inlet I (4.1); the lower end is provided with a discharge outlet I (4.2). The medium-concentration porridge mixing tank (4) is provided with a stirring mechanism (15) with 4 to 8 layers of spiral stirring blades.

5. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The spiral mixer (3) and the medium-concentration porridge mixing tank (4) are an integral structure, and the discharge end of the spiral mixer (3) is connected to the feed end of the medium-concentration porridge mixing tank (4).

6. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The steam pipe (9) is located near the medium-concentration porridge mixing tank (4); the oxygen pipe (11) is located at the rear end of the steam pipe (9).

7. The oxidative depolymerization system for fiber production according to claim 5, characterized in that: The steam pipe (9) is provided with multiple steam inlets (16), and the steam pipe (9) is connected to the steam supply pipeline (10) through the steam inlets (16).

8. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The bottom of the medium-concentration porridge mixing tank (4) is equipped with a porridge pump (17).

9. The oxidative depolymerization system for fiber production according to claim 1, characterized in that: The discharge end of the oxygen-alkali reactor (5) is connected to the impregnation tank (19) via pipe III (18), and the impregnation tank (19) is connected to the alkali supply pipeline (6).

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