Viscose staple fiber acid bath crystallization system and method

Abstract

The invention relates to the technical field of viscose staple fiber production, in particular to a viscose staple fiber acid bath crystallization system and method. Comprising a multi-stage bath lotion preheating assembly, a multi-stage evaporation assembly, an acid bath evaporation chamber, a mother liquor tank and an acid bath bottom groove, an acid bath outlet of the acid bath evaporation chamber is communicated with an inlet of a multi-stage preheater, the acid bath enters the evaporation chamber for flash evaporation after being heated by a heater, secondary steam after flash evaporation enters the pre-heaters at all stages, and the acid bath subjected to multi-stage evaporation enters a mother liquor tank; the mother liquor tank is communicated with a reverse suction inlet of the acid bath evaporation chamber; overflow of the mother liquor tank is communicated with the acid bath bottom groove, and a vertical storage tank is further arranged on a pipeline for communicating the mother liquor tank with the acid bath bottom groove. The acid bath falling into the mother liquor tank enters the vertical storage tank and then enters the acid bath bottom tank under the controllable flow, so that the fluctuation of the acid bath composition can be slowed down; by adding the preheater and the evaporation chamber, the acid bath concentration and sodium sulfate separation effects are better, the evaporation steam-water ratio is effectively reduced, and the purposes of reducing energy consumption and cost are achieved.

Description

Technical Field

[0001] The invention relates to the technical field of viscose staple fiber production, and in particular to a viscose staple fiber acid bath crystallization system and method. Background Art

[0002] Acid bath is the most commonly used coagulation bath in the production of viscose staple fibers. The production process is mainly the reaction of viscose and acid bath. The main components of viscose are cellulose xanthate, alkali and water. The reaction process is the decomposition of cellulose xanthate and acid-base neutralization. The main and side reactions generate a large amount of water, which is dissolved in the acid bath. The acid bath can be recycled through mixing. The acid bath needs to remove water during the mixing process. Crystallization is a process of removing the water introduced during the spinning process by evaporation under vacuum to precipitate sodium sulfate crystals.

[0003] In the current process, the acid bath can be recycled to saturate the acid bath with sodium sulfate and crystallize out. However, the heating and evaporation efficiency is low, and the steam consumption of the crystallization process is high, resulting in energy waste.

[0004] It can be further optimized to further reduce energy consumption and improve secondary steam utilization. Therefore, research and development of new methods to reduce the flash steam water ratio during acid bath evaporation can reduce energy consumption and ensure the quality of spinning products.

[0005] In addition, the existing crystallization process has problems such as large fluctuations in the acid bath composition and short life of the system equipment. Summary of the invention

[0006] The technical problem to be solved by the present invention is to provide a system and method for acid bath crystallization of viscose staple fibers, so as to solve the problems of high steam-water ratio and large fluctuation of acid bath composition in the prior art.

[0007] The technical solution of the present invention to solve the above technical problems is as follows:

[0008] The present invention provides a viscose staple fiber acid bath crystallization system, comprising a multi-stage thermal component, a heating component, a multi-stage evaporation component, an acid bath evaporation chamber, a mother liquid tank and an acid bath bottom tank;

[0009] The acid bath outlet of the acid bath evaporation chamber is communicated with the inlet of the multi-stage preheater, the outlet of the preheater is communicated with the inlet of the multi-stage evaporation assembly, the acid outlet of the multi-stage evaporation assembly is communicated with the mother liquid tank; the mother liquid tank is also communicated with the reverse suction port of the acid bath evaporation chamber;

[0010] The mother liquid tank is communicated with the acid bath bottom tank, and a vertical storage tank is also arranged on the pipeline communicating the mother liquid tank and the acid bath bottom tank.

[0011] Based on the above technical solution, the present invention can also be improved as follows.

[0012] Furthermore, an agitator is installed in the vertical storage tank.

[0013] Furthermore, the multi-stage heating component includes a plurality of preheaters connected in sequence, and the multi-stage evaporation component includes a plurality of evaporation chambers connected in sequence; each of the preheaters is connected to one of the evaporation chambers via a secondary steam pipe.

[0014] Furthermore, the number of the preheaters is 10-13, and the number of the evaporation chambers is 10-15.

[0015] Furthermore, two adjacent evaporation chambers are connected via a peracid tube, an inlet of the peracid tube is connected to the bottom of one evaporation chamber, and an outlet of the peracid tube is connected to the side wall of another evaporation chamber.

[0016] Furthermore, a foamer is installed on the top of the evaporation chamber and the acid bath evaporation chamber.

[0017] Furthermore, the foamer is a hollow cylindrical structure, and three layers of baffles are installed in the foamer. The three layers of baffles are arranged at intervals along the axial direction of the foamer and staggered along the radial direction of the foamer; the baffles are made of rubber-lined steel.

[0018] Furthermore, it also includes a concentrated acid tank, which is connected to the mother liquid tank and the acid bath bottom tank respectively.

[0019] Furthermore, it also includes a crystallization tank, which is connected to the acid bath inlet of the acid bath evaporation chamber, and the crystallization tank is also connected to the flash acid removal device.

[0020] The present invention also provides a viscose staple fiber acid bath crystallization method, which adopts the above-mentioned system to carry out acid bath crystallization.

[0021] The beneficial effects of the present invention are:

[0022] (1) In the viscose staple fiber acid bath crystallization system of the present invention, the acid bath solution falling into the mother liquid tank enters the vertical storage tank and then enters the acid bath bottom tank through a controllable flow rate, thereby slowing down the fluctuation of the acid bath composition;

[0023] (2) The viscose staple fiber acid bath crystallization system of the present invention, the vertical storage tank can reduce the influence of the concentrated acid bath on the system acid bath composition during crystallization conversion;

[0024] (3) The viscose staple fiber acid bath crystallization system of the present invention can achieve better concentration and crystallization effects of the acid bath by providing multiple preheaters and multiple evaporation chambers, while effectively reducing the steam-water ratio, thereby achieving the purpose of reducing energy consumption and costs;

[0025] (4) The viscose staple fiber acid bath crystallization system of the present invention also has the advantage of long service life;

[0026] (5) The viscose staple fiber acid bath crystallization method of the present invention has the advantages of low energy consumption and low cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a structural schematic diagram of the viscose staple fiber acid bath crystallization system of the present invention;

[0028] Figure 2 This is a schematic diagram of the structure of the 16-effect crystallization system of Example 2, a viscose staple fiber acid bath crystallization system of the present invention;

[0029] Figure 3 It is a cross-sectional view of a foamer in the viscose staple fiber acid bath crystallization system of the present invention.

[0030] In the accompanying drawings, the components represented by the reference numerals are listed as follows:

[0031] 1. Multi-stage heating assembly; 11. Preheater;

[0032] 2. Multi-stage evaporation assembly; 21. Evaporation chamber; 22. Acid bath evaporation chamber;

[0033] 3. Acid pipe; 4. Secondary steam pipe;

[0034] 5. Foam puff; 51. First cleaning port; 52. Second cleaning port; 53. Evaporation chamber interface; 54. Upper port; 55. Secondary steam interface; 56. Baffle;

[0035] 6. Mother liquor tank; 7. Acid bath bottom tank; 8. Vertical storage tank; 9. Agitator; 10. Flash acid removal device;

[0036] 12. Concentrated acid tank; 13. Crystallization tank. DETAILED DESCRIPTION

[0037] The principles and features of the present invention are described below in conjunction with the accompanying drawings. The examples given are only used to explain the present invention and are not used to limit the scope of the present invention.

[0038] like Figure 1-3 As shown, the viscose staple fiber acid bath crystallization system of the present invention comprises a multi-stage heating component 1, a multi-stage evaporation component 2, an acid bath evaporation chamber 22, a mother liquid tank 6 and an acid bath bottom tank 7; the acid bath outlet of the acid bath evaporation chamber 22 is connected to the inlet of the multi-stage heating component 1, the outlet of the multi-stage heating component 1 is connected to the inlet of the multi-stage evaporation component 2, and the acid outlet of the multi-stage evaporation component 2 is connected to the mother liquid tank 6; the mother liquid tank 6 is also connected to the reverse suction inlet of the acid bath evaporation chamber 22; the mother liquid tank 6 is connected to the acid bath bottom tank 7, and a vertical storage tank 8 is also provided on the pipeline connecting the mother liquid tank 6 and the acid bath bottom tank 7.

[0039] In the viscose staple fiber acid bath system of the present invention, a vertical storage tank 8 is arranged between the mother liquid tank 6 and the acid bath bottom tank 7, and the vertical storage tank 8 is connected with the mother liquid tank 6, so that the acid bath solution falling into the mother liquid tank 6 enters the vertical storage tank 8 and then enters the acid bath bottom tank 7 at a controllable flow rate, thereby slowing down the fluctuation of the acid bath composition, so that the sodium sulfate concentration in the spinning acid bath composition fluctuates within a range of 0-7 g / L.

[0040] Preferably, a back-suction valve is provided on the pipeline connecting the mother liquor tank 6 and the back-suction port of the acid bath evaporation chamber 22, which can open or close the connection between the two to perform crystallization conversion, wherein the conversion means that the acid in the mother liquor tank 6 is reversely sucked into the acid bath evaporation chamber 22, or the acid in the mother liquor tank 6 can be directly allowed to enter the vertical storage tank 8.

[0041] Preferably, an agitator 9 is installed in the vertical storage tank 8; by providing the agitator 9, when the crystallization conversion occurs, the concentrated acid bath enters the vertical storage tank 8, and then this part of the acid bath is gradually transported to the acid bath circulation system under a controllable flow rate, which can reduce the influence of the concentrated acid bath on the acid bath composition of the acid bath circulation system during the crystallization conversion.

[0042] Preferably, a liquid outlet is provided at the bottom of the vertical storage tank 8 , which is connected to the acid bath bottom tank 7 ; arranging the liquid outlet at the bottom can further increase the buffering effect of the vertical storage tank 8 .

[0043] Preferably, a circulation pump is provided on the pipeline connecting the acid bath outlet of the acid bath evaporation chamber 22 and the inlet of the multi-stage heating assembly 1 .

[0044] In the system of the present invention, the multi-stage heating component 1 includes a plurality of preheaters 11 connected in sequence, and the multi-stage evaporation component 2 includes a plurality of evaporation chambers 21 connected in sequence; each preheater 11 is connected to an evaporation chamber 21 through a secondary steam pipe 4; by providing a plurality of preheaters 11 and a plurality of evaporation chambers 21, the utilization rate of the secondary steam can be effectively improved, the concentration and crystallization effects of the acid bath can be better, and at the same time, the evaporation steam-water ratio can be effectively reduced, thereby achieving the purpose of reducing energy consumption and costs.

[0045] Preferably, the preheaters 11 located upstream are used for preheating at a lower temperature, while the preheaters 11 located downstream, the closer to the outlet of the multi-stage heating assembly 1, the higher the temperature, which can reach up to 108°C.

[0046] Preferably, according to the flow direction, multiple preheaters 11 are connected in series, and multiple evaporation chambers 21 are also connected in series. The correspondence between the preheaters 11 and the evaporation chambers 21 is that the preheaters 11 located upstream are sequentially connected one by one from the evaporation chambers 21 located upstream to the evaporation chambers 21 located downstream. The number of evaporation chambers 21 is generally greater than the number of preheaters 11, so several evaporation chambers 21 located at the downstream end are not connected to the preheater 11.

[0047] In addition, in the multi-stage evaporation assembly 2 , the last evaporation chamber 21 downstream is an evaporation chamber for falling acid, which is not connected to any preheater 11 , and the outlet of the evaporation chamber for falling acid is the concentrated acid outlet of the multi-stage evaporation assembly 2 .

[0048] Preferably, two adjacent evaporation chambers 21 are connected through a peracid tube 3, the inlet of the peracid tube 3 is connected to the bottom of one evaporation chamber 21, and the outlet of the peracid tube 3 is connected to the side wall of the other evaporation chamber 21; the outlet of the peracid tube 3 is arranged on the side wall of the evaporation chamber 21, so that the liquid level in the evaporation chamber 21 is raised to form a liquid seal, and the erosion and wear of the bottom of the evaporation chamber is effectively avoided, thereby extending the service life of the equipment.

[0049] Preferably, the number of preheaters 11 is 10-13, and the number of evaporation chambers 21 is 10-15.

[0050] Specifically, according to the number of multi-stage heating components 1 and multi-stage evaporation components 2, the system of the present invention can be divided into a 14-effect crystallization system and a 16-effect crystallization system, wherein the crystallization system is upgraded and improved on the basis of the conventional crystallization system in conventional technology, and three evaporation chambers 21 and preheaters 11 are added, while the 16-effect crystallization system is further optimized on the basis of the 14-effect crystallization system, and two evaporation chambers 21 and preheaters 11 are added; after optimization, the secondary steam utilization rate can be effectively improved, the fresh steam consumption can be reduced, and the sodium sulfate output rate can be increased.

[0051] Preferably, the system of the present invention further comprises a concentrated acid tank 12, which is respectively connected to the mother liquid tank 6 and the acid bath bottom tank 7. Specifically, one outlet of the mother liquid tank 6 is respectively connected to the vertical storage tank 8 and the concentrated acid tank 12, and an adjustable valve is provided on the connected pipelines, so that the acid bath solution flowing out of the mother liquid tank 6 can enter the vertical storage tank 8 or the concentrated acid tank 12. The outlet of the concentrated acid tank 12 is connected to an inlet of the acid bath bottom tank 7, and the outlet of the vertical storage tank 8 is connected to another inlet of the acid bath bottom tank 7, so that the acid bath solutions in both can enter the acid bath bottom tank 7 in a controllable manner.

[0052] Preferably, the mother liquid tank 6 has a high-level liquid outlet and a low-level liquid outlet, wherein the acid bath overflowing from the high level flows to the concentrated acid tank 12 through the high-level liquid outlet. Preferably, it also includes a crystallization tank 13, which is connected to the acid bath inlet of the acid bath evaporation chamber 22, and the crystallization tank 13 is also connected to the flash acid dropping device 10; the acid dropping specific gravity of the flash acid dropping device 10 can be controlled by adjusting the difference between the feed amount and the circulation amount of the flash acid dropping device 10, and the feed composition is preferably controlled between 1.38-1.39. The acid bath after the first concentration is used as a raw material for crystallization, thereby reducing steam consumption and improving the crystallization and nitrate removal effect.

[0053] Preferably, a frothing device 5 is installed on the top of the evaporation chamber 21 and the acid bath evaporation chamber 22, and the frothing device 5 includes a three-layer rubber-lined baffle 56 and a detachable cleaning port.

[0054] like Figure 3 As shown, the frothing device 5 is a hollow cylindrical structure, and its side wall includes a first cleaning port 51, a second cleaning port 52, an evaporation chamber interface 53, an upper port 54 and a secondary steam interface 55; the cleaning device includes a cleaning pipe, a flushing pipe and valves on two pipes. The first cleaning port 51 is connected to the cleaning pipe, the second cleaning port 52 is connected to the cleaning pipe, the evaporation chamber interface 53 is connected to the top of an evaporation chamber 21 or an acid bath evaporation chamber 22, the upper port 54 is an inspection port, and the secondary steam interface 55 is connected to the secondary steam pipe. The inside of the frothing device 5 is provided with three layers of baffles 56 arranged at intervals, and arranged in staggered directions on the left and right, and the baffles 56 are all steel-lined rubber structures; replacing the original corrugated plate in the frothing device 5 with a three-layer steel-lined rubber baffle can reduce crystallization scale.

[0055] When the baffle plate 56 is clogged, it can be cleaned through the first cleaning port 51 and the second cleaning port 52. Specifically, the valve is opened, and the high-temperature condensed water from the workshop enters the frothing device 5 through the second cleaning port 52 or the first cleaning port 51, and the cleaned water enters the evaporation chamber 21 and the acid bath in the acid bath evaporation chamber 22, so as to achieve timely cleaning and ensure the normal operation of the frothing device 5.

[0056] Preferably, the system of the present invention further includes at least one graded pressure reduction tank, and each graded pressure reduction tank is connected to a preheater 11. The graded pressure reduction tank is a conventional setting. In the method of the present invention, the improvement of the graded pressure reduction tank is mainly carried out for the original 11-effect crystallization system. As mentioned above, after the 11-effect crystallization system is improved to the 14-effect crystallization system, three evaporation chambers and a preheater 11 are added, while only one graded pressure reduction tank is provided in the original 11-effect crystallization system. Therefore, after the evaporation chamber and the preheater 11 are added, the graded pressure reduction tank is also added, so that the condensed water of the preheater 11 passes through the original pressure reduction tank and then passes through the graded pressure reduction tank for cooling, and the secondary steam of the graded pressure reduction tank is supplied to the preheater 11 for use, thereby improving the utilization rate of the thermal enthalpy of the condensed water.

[0057] When a 14-effect crystallization system is transformed into a 16-effect crystallization system, since the original 14-effect crystallization system already contains 3 graded pressure reduction tanks, there is no need to add more.

[0058] The viscose staple fiber acid bath crystallization method of the present invention is carried out by adopting the above system.

[0059] The present invention is specifically described below by way of examples.

[0060] Example 1

[0061] This embodiment upgrades the original device to a 14-effect crystallization system. The evaporation chamber 21 and the acid bath evaporation chamber 22 are denoted as V, and the preheater 11 is denoted as A. For the 14-effect crystallization system, the specific structures of the multi-stage heating component 1 and the multi-stage evaporation component 2 are as follows:

[0062] It includes 13 evaporation chambers 21 and 1 acid bath evaporation chamber 22. The evaporation chambers 21 are respectively denoted as V1, V2, V3, V4, V5, V6, V7, V8, V9, V10, V11, V12, and V13, and the acid bath evaporation chamber 22 is denoted as V14. Among them, V3, V4, and V5 are evaporation chambers 21 added to the original 11-effect crystallization system. After the addition, the acid bath evaporation chamber 22 changes from V10 to V13. Correspondingly, since the evaporation chamber 21 is increased by three levels, three preheaters 11 are added on this basis, so that the 14-effect crystallization system specifically includes 11 preheaters 11, which are respectively denoted as A1, A2, A3, A4, A5, A6, A7, A8, A9, A10, and A11.

[0063] In addition, a graded decompression tank is provided on A8, so that the condensed water in the preheater 11 located after A8 passes through the original decompression tank and then passes through the graded decompression tank for cooling, and the secondary steam of the graded decompression tank is supplied to A8 for use, thereby improving the utilization rate of the thermal enthalpy of the condensed water.

[0064] By changing the 11-effect crystallization system to a 14-effect crystallization system, the secondary steam utilization rate was improved, the preheating temperature was increased, the steam consumption was effectively reduced, and the sodium sulfate output rate was increased.

[0065] Example 2

[0066] In this example, the original device is upgraded to a 14-effect crystallization system, and the 14-effect crystallization system and the 16-effect crystallization system are compared respectively.

[0067] like Figure 2 As shown, the evaporation chamber 21 and the acid bath evaporation chamber 22 are marked as V, the preheater 11 is marked as A, including 15 evaporation chambers 21 and 1 acid bath evaporation chamber 22, the evaporation chambers 21 are marked as V1, V2, V3, V4, V5, V6, V7, V8, V9, V10, V11, V12, V13, V14, V15, the acid bath evaporation chamber 22 is marked as V16, Figure 2 V1 and V2 are not shown. Among them, V7 and V8 are evaporation chambers 21 added to the original 14-effect crystallization system. After the addition, the evaporation chamber of the acid is converted from V13 to V15. Correspondingly, since two evaporation chambers 21 are added, two preheaters 11 are added on this basis, so that the 16-effect crystallization system specifically includes 13 preheaters 11, which are respectively denoted as A1, A2, A3, A4, A5, A6, A7, A8, A9, A10, A11, A12, and A13. In actual use, the temperatures of these preheaters 11 are relatively low, and it can be considered that their function is preheating. Figure 2 , A1-A5 are not shown.

[0068] In addition, the 16-effect crystallization system of this embodiment is also provided with heater A0 and heater H ( Figure 2 Both are located downstream of A1 and connected to evaporation chamber V1. The heating temperature of heater A0 and heater H can reach a maximum temperature of 108°C.

[0069] After the transformation to a 16-effect crystallization system, under the same feed and circulation volume, the acid temperature dropped from 53°C to 50°C, and the A1 temperature rose from 84°C to 87°C. The acid was buffered and prepared into an acid bath in vertical tank 8, and the sodium sulfate concentration in the acid bath composition ranged from 344-351g / L. Finally, the fluctuation range of sodium sulfate in the acid bath composition for spinning during crystallization conversion was reduced from 20g / l to less than 7g / L. According to calculations, the steam-water ratio dropped from 0.29t steam / t water to 0.265 steam / t water, which meets the requirement that the steam-water ratio can reduce 0.02-0.08 tons / ton of water. The total annual steam savings: (0.29-0.265)*25*8000=5000 tons, and the annual benefits are 5000*200=1 million yuan.

[0070] In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0071] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0072] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0073] In the description of this specification, the description with reference to the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0074] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0075] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A viscose staple fiber acid bath crystallization system, characterized in that: It comprises a multi-stage heating component (1), a multi-stage evaporation component (2), an acid bath evaporation chamber (22), a mother liquid tank (6) and an acid bath bottom tank (7); The acid bath outlet of the acid bath evaporation chamber (22) is communicated with the inlet of the multi-stage heating assembly (1), the outlet of the multi-stage heating assembly (1) is communicated with the inlet of the multi-stage evaporation assembly (2), the acid outlet of the multi-stage evaporation assembly (2) is communicated with the mother liquid tank (6); the mother liquid tank (6) is also communicated with the reverse suction port of the acid bath evaporation chamber (22); The mother liquid tank (6) is in communication with the acid bath bottom tank (7), and a vertical storage tank (8) is added to the pipeline connecting the mother liquid tank (6) and the acid bath bottom tank (7).

2. A viscose staple fiber acid bath crystallization system according to claim 1, characterized in that: A stirrer (9) is installed in the additional vertical storage tank (8).

3. The viscose staple fiber acid bath crystallization system according to claim 1, characterized in that: The multi-stage heating component (1) comprises a plurality of preheaters (11) connected in sequence, and the multi-stage evaporation component (2) comprises a plurality of evaporation chambers (21) connected in sequence; each of the preheaters (11) is connected to one of the evaporation chambers (21) via a secondary steam pipe (4).

4. A viscose staple fiber acid bath crystallization system according to claim 3, characterized in that: The number of the preheaters (11) is 10-13, and the number of the evaporation chambers (21) is 10-15.

5. The viscose staple fiber acid bath crystallization system according to claim 3, characterized in that: Two adjacent evaporation chambers (21) are connected via a peracid tube (3), the inlet of the peracid tube (3) is connected to the bottom of one evaporation chamber (21), and the outlet of the peracid tube (3) is connected to the side wall of the other evaporation chamber (21).

6. A viscose staple fiber acid bath crystallization system according to claim 3, characterized in that: A foamer (5) is installed on the top of the evaporation chamber (21) and the acid bath evaporation chamber (22).

7. A viscose staple fiber acid bath crystallization system according to claim 6, characterized in that: The foamer (5) is a hollow columnar structure. Three layers of baffles (56) are installed in the foamer (5). The three layers of baffles (56) are arranged at intervals along the axial direction of the foamer (5) and are arranged in a staggered manner along the radial direction of the foamer (5). The material of the baffles (56) is steel-lined rubber.

8. A viscose staple fiber acid bath crystallization system according to any one of claims 1 to 7, characterized in that: It also comprises a concentrated acid tank (12), wherein the concentrated acid tank (12) is respectively connected to the mother liquid tank (6) and the acid bath bottom tank (7).

9. A viscose staple fiber acid bath crystallization system according to any one of claims 1 to 7, characterized in that: It also comprises a crystallization tank (13), wherein the crystallization tank (13) is connected to the acid bath inlet of the acid bath evaporation chamber (22), and the crystallization tank (13) is also connected to the flash acid evaporation device (10).

10. A method for crystallizing viscose staple fibers in an acid bath, characterized in that: Acid bath crystallization is carried out using the system as described in any one of claims 1 to 9.

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