Primary dealcoholization system for crude alkyl glycoside
By installing a gas-liquid separator and internal components in the crude alkyl glycoside falling film tubular deethanoler, the problems of low deethanoling rate and high alkyl glycoside residue in the existing technology are solved, and efficient removal of fatty alcohols and recovery of alkyl glycosides are achieved.
Patent Information
- Application Number
- CN202520109969.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-01-17
- Publication Date
- 2025-11-14
- Estimated Expiration
- 2035-01-17
AI Technical Summary
The existing crude alkyl glycoside primary dealcoholization system has a low removal rate of fatty alcohols and a high residual amount of alkyl glycosides, which leads to an increased load on the subsequent secondary dealcoholization process.
A gas-liquid separator and internal components are installed in the crude alkyl glycoside falling film tubular dehydrogenator. The gas-liquid separator is used to recover alkyl glycosides, and the internal components are used to stabilize the material distribution and reduce the effects of turbulence.
It improves the removal rate of fatty alcohols and the total yield of alkyl glycosides, reduces the residual amount of alkyl glycosides in fatty alcohols, and reduces the load on subsequent processes.
Smart Images
Figure CN223542452U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to a primary de-alcoholization system for crude alkyl glycosides. Background Technology
[0002] There are two main process routes for producing alkyl glycosides: a two-step method (also known as the acetal exchange method or glycoside transglycosylation method) and a one-step method (also known as the direct method). The one-step method involves reacting fatty alcohols (usually C8-18 fatty alcohols) with glucose in the presence of an acidic catalyst to obtain alkyl glycosides. Since this reaction is reversible, an excess of fatty alcohol is required to ensure complete conversion of glucose to glycosides. Therefore, the product contains a large amount of unreacted fatty alcohol. After neutralization, this unreacted fatty alcohol needs to be removed from the product. The removal of fatty alcohol typically requires a two-stage dealcoholization system: a falling film dealcoholization system for the first stage and a scraped-plate dealcoholization system for the second stage. Currently, the mainstream unit for primary alcohol removal systems is the tubular falling film alcohol removal unit. After crude glycosides containing unreacted fatty alcohols enter the unit, the material is distributed to the tubular shells via overflow. The material then flows downwards from the inner wall of the tubes in the form of a liquid film. High-temperature heat transfer oil is circulated outside the tubes for heating, and the entire unit is under negative pressure (-98 to -99 kPa). By reducing the pressure drop, the boiling point of the fatty alcohols is lowered, allowing them to evaporate and be removed from the crude glycosides. However, the fatty alcohol vapor exiting the falling film alcohol removal unit carries a significant amount of alkyl glycosides, which will result in alkyl glycoside loss if not recovered. In addition, existing crude alkyl glycoside dealcoholizers use a design where the crude alkyl glycoside inlet is lower than the opening on the dealcoholizing tube, thereby distributing the crude alkyl glycoside between the dealcoholizing tubes through overflow. However, this distribution method can cause uneven spreading of the crude alkyl glycoside on the inner wall of the dealcoholizing tube due to fluctuations in the feed flow rate at the crude alkyl glycoside inlet or turbulence of the material. The primary fatty alcohol removal rate of crude alkyl glycoside needs to be improved. The removal rate of fatty alcohol in existing primary dealcoholizing systems is generally 65-75%, which is low and leads to a significant increase in the load of the subsequent secondary dealcoholizing process. Utility Model Content
[0003] The technical problem this utility model aims to solve is: one of the problems is the high residual alkyl glycoside content in the fatty alcohols recovered by existing crude alkyl glycoside primary dealcoholization systems. This invention provides a new crude alkyl glycoside primary dealcoholization system with the advantage of low residual alkyl glycoside content in the recovered fatty alcohols. Alternatively,
[0004] The second technical problem is the low removal rate of fatty alcohols in existing crude alkyl glycoside primary dealcoholization systems. To address this, a new crude alkyl glycoside primary dealcoholization system is provided, which has the advantages of high dealcoholization efficiency and low fatty alcohol residue.
[0005] To solve one of the above-mentioned technical problems, the technical solution of this utility model is as follows:
[0006] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, the dealcoholization tube heating area is located between the upper and lower tube sheets, and the gas-liquid separation area within the dealcoholizer is located in the lower tube sheet. Below the plate; a crude alkyl glycoside inlet (110) is provided in the crude alkyl glycoside fabrication area; the container is provided with a de-alcoholizing pipe (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing pipe communicates with the crude alkyl glycoside fabrication area, and the lower opening of the de-alcoholizing pipe communicates with the gas-liquid separation area inside the de-alcoholizer; the gas-liquid separation area inside the tubular de-alcoholizer is provided with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104); the de-alcoholizing system is provided with a fatty alcohol condenser (200) for condensing the alcohol vapor generated by the tubular de-alcoholizer into liquid;
[0007] The crude alkyl glycoside primary de-alcoholization system includes a gas-liquid separator (600), with the alcohol vapor outlet (104) of the tubular de-alcoholizer entering the inlet of the gas-liquid separator, and the gas phase alcohol outlet (601) of the gas-liquid separator entering the feed inlet of the fatty alcohol condenser.
[0008] To solve the second technical problem mentioned above, the technical solution of this utility model is as follows:
[0009] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, the dealcoholization tube heating area is located between the upper and lower tube sheets, and the gas-liquid separation area within the dealcoholizer is located below the lower tube sheet. The zone is equipped with a crude alkyl glycoside inlet (110); the container is equipped with a de-alcoholizing pipe (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing pipe is connected to the crude alkyl glycoside feeding zone, and the upper opening of the de-alcoholizing pipe is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing pipe is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tube de-alcoholizer is equipped with a tube de-alcoholizer alkyl glycoside material discharge channel (105) and a tube de-alcoholizer alcohol vapor outlet (104); the de-alcoholizing system is equipped with a fatty alcohol condenser (200) for condensing the alcohol vapor generated by the tube de-alcoholizer into liquid.
[0010] An internal component (112) is provided at the opening of the deethanolating tube. The internal component (112) extends into the deethanolating tube from the opening. The side of the internal component has the shape of a rotating body side. The top diameter of the rotating body is smaller than the bottom diameter. The lower edge of the rotating body side has a gap with the inner wall of the deethanolating tube.
[0011] In the above technical solution, the rotating body is preferably a cone or a frustum, and more preferably a frustum.
[0012] To achieve the purpose of condensing the alcohol vapor generated by the tubular alcohol dehydrogenator into liquid, the alcohol vapor outlet (104) of the tubular alcohol dehydrogenator can be directly fed into the feed inlet of the fatty alcohol condenser (200). Preferably, a gas-liquid separator (600) is set between the alcohol vapor outlet (104) of the tubular alcohol dehydrogenator and the feed inlet of the fatty alcohol condenser. The alcohol vapor outlet (104) of the tubular alcohol dehydrogenator is fed into the inlet of the gas-liquid separator, and the gas phase alcohol outlet (601) of the gas-liquid separator is fed into the feed inlet of the fatty alcohol condenser.
[0013] In the above technical solution, the gas-liquid separator can be selected from at least one of the following separators: free gas-liquid static separator, centrifugal gas-liquid separator, cyclone gas-liquid separator, filter gas-liquid separator, floating gas-liquid separator, electrostatic precipitator gas-liquid separator, packing separator, and baffle separator.
[0014] In the above technical solution, the preferred method is to input the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator into the outlet (603) of the gas-liquid separator recovering alkyl glycoside.
[0015] In the above technical solution, it is preferable that the axis of the rotating body coincides with the axis of the deethanolination tube.
[0016] In the above technical solution, if the angle between the generatrix of the rotating body and the axis of the deethanolination tube is α, then preferably α is greater than 0° and less than 90°, for example, but not limited to 1°, 2°, 3°, 4°, 5°, 10°, 15°, 20°, 25°, 30°, 35°, 40°, 45°, 50°, 55°, 60°, 65°, 70°, 75°, 80°, 85°, etc., more preferably 5° to 30°.
[0017] In the above technical solution, preferably, the bottom of the inner component has an axis line from the lower edge line of the side of the rotating body toward the center line of the de-alcoholizing tube and an upward curved surface.
[0018] In the above technical solution, the included angle between the curved surface and the side of the rotating body is β, where β is greater than 0° and less than 90°-α.
[0019] In the above technical solution, it is preferred that the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator is equipped with an alkyl glycoside discharge pump (500).
[0020] In the above technical solution, it is preferable to input the condenser outlet (202) into the vacuum buffer tank (300) inlet.
[0021] In the above technical solution, it is preferable that the vacuum buffer tank (300) is equipped with a vacuum interface (302).
[0022] In the above technical solution, it is preferred that the vacuum buffer tank (300) be provided with a vacuum buffer tank outlet (301).
[0023] In the above technical solution, it is preferred that the outlet (301) of the vacuum buffer tank is connected to the inlet of the vacuum buffer tank discharge pump (400).
[0024] The beneficial effects of the above-mentioned utility model are:
[0025] 1. The gas-liquid separator reduces the loss caused by the entrainment of alkyl glycosides in fatty alcohols and improves the overall yield of alkyl glycosides.
[0026] 2. The above-mentioned internal components, due to their inclined sides and the slits between them and the inner wall of the dehydrogenation tube, suppress the uneven spreading of crude alkyl glycosides on the inner wall of the dehydrogenation tube caused by fluctuations in the feed flow of crude alkyl glycosides or turbulence of the material, thereby improving the fatty alcohol removal rate of crude alkyl glycosides.
[0027] 3. The aforementioned raised surface can prevent a small amount of crude alkyl glycosides from being diverted to a surface far from the inner surface of the dealcoholization tube.
[0028] In the utility model specification, the method for measuring the residual amount of alkyl glycosides in fatty alcohols is adopted from Appendix B of GB / T19464-2014. This method can measure both the degree of polymerization and the content of alkyl glycosides.
[0029] In the utility model specification, the mass fraction of fatty alcohols in the crude alkyl glycosides is measured using the method in Appendix A of GB / T19464-2014. The de-alcoholization rate of the primary de-alcoholization system of the crude alkyl glycosides is calculated based on the mass fraction of fatty alcohols, using the following formula:
[0030] De-alcoholization rate of the crude alkyl glycoside primary de-alcoholization system = ((AB) / A) × 100%
[0031] In the formula: A is the mass fraction of fatty alcohol in the crude alkyl glycoside feed of the primary dealcoholization system, and B is the mass fraction of fatty alcohol in the crude alkyl glycoside discharge of the primary dealcoholization system. Attached Figure Description
[0032] Figure 1 This is a schematic diagram of an existing crude alkyl glycoside primary dehydrogenation system.
[0033] Figure 2This is a schematic diagram of the first embodiment of the present invention.
[0034] Figure 3 yes Figure 1 and Figure 2 An enlarged view of the area indicated by the dashed box a.
[0035] Figure 4 This is a schematic diagram of the second embodiment of the present invention.
[0036] Figure 5 This is a schematic diagram of the third embodiment of the present invention.
[0037] Figure 6 for Figure 4 and Figure 5 An enlarged view of the area shown in the dashed box b.
[0038] In the picture:
[0039] 100 is a falling film tubular alcohol separator; the dashed boxes in a and b indicate enlarged areas; 102 is the upper tube sheet; 103 is the oil bath outlet of the tubular alcohol separator; 104 is the alcohol vapor outlet of the tubular alcohol separator; 105 is the alkyl glycoside material discharge channel of the tubular alcohol separator; 106 is the gas-liquid separation zone inside the tubular alcohol separator; 107 is the lower tube sheet; 108 is the oil bath inlet of the tubular alcohol separator; 109 is the alcohol separator tube; 110 is the crude alkyl glycoside inlet; 111 is the mounting plate used to fix internal components; 112 is the internal components of the tube; 20 0 is the fatty alcohol condenser; 201 is the cooling water outlet; 202 is the condenser outlet; 203 is the cooling water inlet; 300 is the vacuum buffer tank; 301 is the vacuum buffer tank outlet; 302 is the vacuum interface; 400 is the vacuum buffer tank discharge pump; 500 is the alkyl glycoside discharge pump; 600 is the gas-liquid separator; 601 is the gas phase alcohol outlet of the gas-liquid separator; 602 is the oil bath outlet of the gas-liquid separator; 603 is the alkyl glycoside recovery outlet of the gas-liquid separator; 604 is the oil bath inlet of the gas-liquid separator. Detailed Implementation
[0040] In a specific embodiment, the crude alkyl glycoside feed for the dealcoholizer is obtained by glycosylation reaction of C12-14 fatty alcohols with glucose, followed by neutralization and filtration to obtain crude glycosides. The main components, by weight, are alkyl glycosides (34.5%), fatty alcohols (63.2%), catalyst neutralization products (0.3%), and other impurities (2%).
[0041] 1. Existing technical implementation methods
[0042] See Figure 1 and Figure 3 .
[0043] 1.1 Existing Technology Implementation Methods
[0044] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, and the dealcoholization tube heating area is located between the upper and lower tube sheets. The gas-liquid separation area within the dealcoholizer... The liquid separation zone is located below the lower tube sheet; the crude alkyl glycoside feeding zone is provided with a crude alkyl glycoside inlet (110); the container is provided with a de-alcoholizing tube (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing tube is connected to the crude alkyl glycoside feeding zone, and the upper opening of the de-alcoholizing tube is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing tube is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tubular de-alcoholizer is provided with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104).
[0045] The alcohol vapor outlet (104) of the tubular alcohol dehydrogenator is directly fed into the feed inlet of the fatty alcohol condenser (200).
[0046] An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
[0047] The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
[0048] The vacuum buffer tank (300) is equipped with a vacuum interface (302).
[0049] The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
[0050] The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.
[0051] 1.2 Examples of Existing Technology Implementation
[0052] 1.2.1 Equipment geometric parameters
[0053] 1.2.1.1 Geometric parameters of the crude alkyl glycoside falling film tubular dehydrogenator
[0054] Container: The dehydrogenator container is cylindrical in the middle and hemispherical at both ends. The cylinder is 6m high and 1m in diameter. The lower surface of the lower tube sheet is flush with the lower edge of the cylinder, and the upper surface of the upper tube sheet is 50mm from the upper edge of the cylinder.
[0055] De-alcoholization tube: The height of the de-alcoholization tube is 6m, the inner diameter is 45mm, and the number of de-alcoholization tubes is 307; the lower opening of the de-alcoholization tube is flush with the lower surface of the lower tube sheet, and the upper opening of the de-alcoholization tube is 50mm higher than the upper surface of the upper tube sheet.
[0056] 1.2.1.2 Geometric parameters of fatty alcohol condenser (200)
[0057] Horizontal shell-and-tube condenser, total length 6m, total heat exchange area 120m² 2 .
[0058] 1.2.2, Process Parameters of the Example
[0059] The crude glycosides enter the dealcoholizer at a flow rate of 800 kg / h. The oil temperature in the dealcoholizer is controlled at 165°C, the circulating water temperature in the dealcoholizer condenser is set at 25°C, and the absolute pressure of the vacuum system is 3 kPa.
[0060] Tests showed that after primary alcohol removal, the alcohol removal rate of crude glycosides was 73%, and the residual alkyl glycosides in the recovered fatty alcohols were 8.0%.
[0061] 2. The first embodiment of this utility model
[0062] See Figure 2 and Figure 3 .
[0063] 2.1 Technical solution of the first embodiment of this utility model
[0064] Except for the addition of a gas-liquid separator, everything else is the same as in 1.1. Specifically:
[0065] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, and the dealcoholization tube heating area is located between the upper and lower tube sheets. The gas-liquid separation area within the dealcoholizer... The liquid separation zone is located below the lower tube sheet; the crude alkyl glycoside feeding zone is provided with a crude alkyl glycoside inlet (110); the container is provided with a de-alcoholizing tube (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing tube is connected to the crude alkyl glycoside feeding zone, and the upper opening of the de-alcoholizing tube is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing tube is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tubular de-alcoholizer is provided with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104).
[0066] The crude alkyl glycoside primary dealcoholization system includes a gas-liquid separator (600), with the alcohol vapor outlet (104) of the tubular dealcoholizer entering the gas-liquid separator inlet, and the gas phase alcohol outlet (601) of the gas-liquid separator entering the fatty alcohol condenser inlet. The alkyl glycoside recovery outlet (603) of the gas-liquid separator enters the alkyl glycoside material discharge channel (105) of the tubular dealcoholizer.
[0067] An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
[0068] The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
[0069] The vacuum buffer tank (300) is equipped with a vacuum interface (302).
[0070] The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
[0071] The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.
[0072] 2.2 First Embodiment of the Present Invention
[0073] 2.2.1 Equipment geometric parameters
[0074] 2.2.1.1 Geometric parameters of crude alkyl glycoside falling film tubular dehydrogenator
[0075] Same as 1.2.1.1, specifically:
[0076] Container: The dehydrogenator container is cylindrical in the middle and hemispherical at both ends. The cylinder is 6m high and 1m in diameter. The lower surface of the lower tube sheet is flush with the lower edge of the cylinder, and the upper surface of the upper tube sheet is 50mm from the upper edge of the cylinder.
[0077] De-alcoholization tube: The height of the de-alcoholization tube is 6m, the inner diameter is 45mm, and the number of de-alcoholization tubes is 307; the lower opening of the de-alcoholization tube is flush with the lower surface of the lower tube sheet, and the upper opening of the de-alcoholization tube is 50mm higher than the upper surface of the upper tube sheet.
[0078] 2.2.1.2 Geometric parameters of the fatty alcohol condenser (200)
[0079] Same as 1.2.1.2. Specifically:
[0080] Horizontal shell-and-tube condenser, total length 6m, total heat exchange area 120m² 2 .
[0081] 2.2.1.3 Geometric parameters of the gas-liquid separator (600)
[0082] The gas-liquid separator (600) is a gas-liquid static separator with a diameter of 1.1m and a height of 5.4m, and is equipped with heat-conducting oil for heating.
[0083] 2.2.2 Process Parameters of the Example
[0084] Except for the addition of process parameters at the gas-liquid separator, everything else is the same as in 1.2.2. Specifically:
[0085] Crude glycosides enter the dealcoholizer at a flow rate of 800 kg / h. The oil temperature in the dealcoholizer is controlled at 165°C, the circulating water temperature in the dealcoholizer condenser is set at 25°C, and the absolute pressure of the vacuum system is 3 kPa. The heat transfer oil used to heat the gas-liquid static separator is at a temperature of 165°C.
[0086] Tests showed that after primary alcohol removal, the alcohol removal rate of crude glycosides was 72%, and the residual alkyl glycosides in the recovered fatty alcohols were 0.1%.
[0087] 3. The second embodiment of this utility model
[0088] See Figure 4 and Figure 6 .
[0089] 3.1 Technical solution of the second embodiment of this utility model
[0090] Except for the installation of an internal component (112) at the opening of the deethanolination tube, it is the same as 1.1. Specifically:
[0091] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, and the dealcoholization tube heating area is located between the upper and lower tube sheets. The gas-liquid separation area within the dealcoholizer... The liquid separation zone is located below the lower tube sheet; the crude alkyl glycoside feeding zone is provided with a crude alkyl glycoside inlet (110); the container is provided with a de-alcoholizing tube (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing tube is connected to the crude alkyl glycoside feeding zone, and the upper opening of the de-alcoholizing tube is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing tube is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tubular de-alcoholizer is provided with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104).
[0092] The alcohol vapor outlet (104) of the tubular alcohol dehydrogenator is directly fed into the feed inlet of the fatty alcohol condenser (200).
[0093] An internal component (112) is provided at the opening of the deethanolating tube. The internal component (112) extends into the deethanolating tube from the opening. The side of the internal component has the shape of a frustum. The top diameter of the frustum is smaller than the bottom diameter. The lower edge of the frustum has a gap with the inner wall of the deethanolating tube.
[0094] The centerline of the frustum coincides with the centerline of the deethanolination tube.
[0095] The angle between the generatrix of the frustum and the axis of the deethanolination tube is α, where α is greater than 0° and less than 90°, and preferably α is 5° to 30°.
[0096] The bottom of the inner component has an axis line extending from the lower edge of the side of the frustum toward the deethanolination tube and an upward-curving surface.
[0097] The angle between the curved surface and the side of the frustum is β, where β is greater than 0° and less than 90°-α.
[0098] An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
[0099] The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
[0100] The vacuum buffer tank (300) is equipped with a vacuum interface (302).
[0101] The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
[0102] The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.
[0103] 3.2 Second Embodiment of the Present Invention
[0104] 3.2.1 Equipment geometric parameters
[0105] 3.2.1.1 Geometric parameters of crude alkyl glycoside falling film tubular dehydrogenator
[0106] Same as 1.2.1.1. Specifically:
[0107] Container: The dehydrogenator container is cylindrical in the middle and hemispherical at both ends. The cylinder is 6m high and 1m in diameter. The lower surface of the lower tube sheet is flush with the lower edge of the cylinder, and the upper surface of the upper tube sheet is 50mm from the upper edge of the cylinder.
[0108] De-alcoholization tube: The height of the de-alcoholization tube is 6m, the inner diameter is 45mm, and the number of de-alcoholization tubes is 307; the lower opening of the de-alcoholization tube is flush with the lower surface of the lower tube sheet, and the upper opening of the de-alcoholization tube is 50mm higher than the upper surface of the upper tube sheet.
[0109] 3.2.1.2 Geometric parameters of the fatty alcohol condenser (200)
[0110] Same as 1.2.1.2. Specifically:
[0111] Horizontal shell-and-tube condenser, total length 6m, total heat exchange area 120m² 2 .
[0112] 3.2.1.4 Geometric dimensions of internal pipe components
[0113] The upper edge of the side of the frustum is flush with the opening of the deethanolination tube; the frustum is 50mm high, the width of the slit between the lower edge of the side of the frustum and the inner wall of the deethanolination tube is 5mm, the axis of the frustum coincides with the axis of the deethanolination tube, the angle α between the generatrix of the frustum and the axis of the deethanolination tube is 10°, and the bottom of the inner component has a raised curved surface extending from the lower edge of the side of the frustum toward the axis of the deethanolination tube and upward, the angle β between the curved surface and the side of the frustum is 30°.
[0114] 3.2.2 Process Parameters of the Example
[0115] The process parameters are the same as in 1.2.2. Specifically:
[0116] The crude glycosides are fed into the dehydrogenator at a flow rate of 800 kg / h. The oil temperature in the dehydrogenator is controlled at 165°C for heating and evaporation dehydrogenation. The circulating water temperature in the dehydrogenator condenser is set at 25°C, and the absolute pressure of the vacuum system is 3 kPa.
[0117] Tests showed that after primary alcohol removal, the alcohol removal rate of crude glycosides was 93%, and the residual alkyl glycosides in the recovered fatty alcohols was 7.8%.
[0118] 4. The third embodiment of this utility model
[0119] See Figure 5 and Figure 6 .
[0120] 4.1 Technical solution of the third embodiment of this utility model
[0121] Except for the installation of an internal component (112) at the opening of the deethanolination tube, it is the same as 2.1. Specifically:
[0122] A primary alkyl glycoside dealcoholization system includes a crude alkyl glycoside falling film tubular dealcoholizer (100). The dealcoholizer includes a container with an upper tube sheet (102) and a lower tube sheet (107) inside. The container includes three regions separated by the upper and lower tube sheets: a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer. The crude alkyl glycoside distribution area is located above the upper tube sheet, and the dealcoholization tube heating area is located between the upper and lower tube sheets. The gas-liquid separation area within the dealcoholizer... The liquid separation zone is located below the lower tube sheet; the crude alkyl glycoside feeding zone is provided with a crude alkyl glycoside inlet (110); the container is provided with a de-alcoholizing tube (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing tube is connected to the crude alkyl glycoside feeding zone, and the upper opening of the de-alcoholizing tube is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing tube is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tubular de-alcoholizer is provided with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104).
[0123] The crude alkyl glycoside primary dealcoholization system includes a gas-liquid separator (600), with the alcohol vapor outlet (104) of the tubular dealcoholizer entering the gas-liquid separator inlet, and the gas phase alcohol outlet (601) of the gas-liquid separator entering the fatty alcohol condenser inlet. The alkyl glycoside recovery outlet (603) of the gas-liquid separator enters the alkyl glycoside material discharge channel (105) of the tubular dealcoholizer.
[0124] An internal component (112) is provided at the opening of the deethanolating tube. The internal component (112) extends into the deethanolating tube from the opening. The side of the internal component has the shape of a frustum. The top diameter of the frustum is smaller than the bottom diameter. The lower edge of the frustum has a gap with the inner wall of the deethanolating tube.
[0125] The centerline of the frustum coincides with the centerline of the deethanolination tube.
[0126] The angle between the generatrix of the frustum and the axis of the deethanolination tube is α, where α is greater than 0° and less than 90°, and preferably α is 5° to 30°.
[0127] The bottom of the inner component has an axis line extending from the lower edge of the side of the frustum toward the deethanolination tube and an upward-curving surface.
[0128] The angle between the curved surface and the side of the frustum is β, where β is greater than 0° and less than 90°-α.
[0129] An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
[0130] The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
[0131] The vacuum buffer tank (300) is equipped with a vacuum interface (302).
[0132] The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
[0133] The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.
[0134] 4.2 Third Embodiment of the Present Invention
[0135] 4.2.1 Equipment geometric parameters
[0136] 4.2.1.1 Geometric parameters of the crude alkyl glycoside falling film tubular dehydrogenator
[0137] Same as 1.2.1.1. Specifically:
[0138] Container: The dehydrogenator container is cylindrical in the middle and hemispherical at both ends. The cylinder is 6m high and 1m in diameter. The lower surface of the lower tube sheet is flush with the lower edge of the cylinder, and the upper surface of the upper tube sheet is 50mm from the upper edge of the cylinder.
[0139] De-alcoholization tube: The height of the de-alcoholization tube is 6m, the inner diameter is 45mm, and the number of de-alcoholization tubes is 307; the lower opening of the de-alcoholization tube is flush with the lower surface of the lower tube sheet, and the upper opening of the de-alcoholization tube is 50mm higher than the upper surface of the upper tube sheet.
[0140] 4.2.1.2 Geometric parameters of the fatty alcohol condenser (200)
[0141] Same as 1.2.1.2. Specifically:
[0142] Horizontal shell-and-tube condenser, total length 6m, total heat exchange area 120m² 2 .
[0143] 4.2.1.3 Geometric parameters of the gas-liquid separator (600)
[0144] Same as 2.2.1.3. Specifically:
[0145] The gas-liquid separator (600) is a gas-liquid static separator with a diameter of 1.1m and a height of 5.4m, and is equipped with heat-conducting oil for heating.
[0146] 4.2.1.4 Geometric dimensions of internal pipe components
[0147] Same as 3.2.1.4. Specifically:
[0148] The upper edge of the side of the frustum is flush with the opening of the deethanolination tube; the frustum is 50mm high, the width of the slit between the lower edge of the side of the frustum and the inner wall of the deethanolination tube is 5mm, the axis of the frustum coincides with the axis of the deethanolination tube, the angle α between the generatrix of the frustum and the axis of the deethanolination tube is 10°, and the bottom of the inner component has a raised curved surface extending from the lower edge of the side of the frustum toward the axis of the deethanolination tube and upward, the angle β between the curved surface and the side of the frustum is 30°.
[0149] 4.2.2, Process Parameters of the Example
[0150] The process parameters are the same as in 2.2.2. Specifically:
[0151] Crude glycosides enter the dealcoholizer at a flow rate of 800 kg / h. The oil temperature in the dealcoholizer is controlled at 165°C, the circulating water temperature in the dealcoholizer condenser is set at 25°C, and the absolute pressure of the vacuum system is 3 kPa. The heat transfer oil used to heat the gas-liquid static separator is at a temperature of 165°C.
[0152] Tests showed that after primary alcohol removal, the alcohol removal rate of crude glycosides was 93%, and the residual alkyl glycosides in the recovered fatty alcohols were 0.1%.
Claims
1. A primary dealcoholization system for crude alkyl glycosides, comprising a crude alkyl glycoside falling film tubular dealcoholizer (100), the dealcoholizer comprising a container, an upper tube sheet (102) and a lower tube sheet (107) disposed within the container, the container comprising three regions separated by the upper and lower tube sheets, the three regions being a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer, the crude alkyl glycoside distribution area being located above the upper tube sheet, the dealcoholization tube heating area being located between the upper and lower tube sheets, and the gas-liquid separation area within the dealcoholizer being located below the lower tube sheet. The container is equipped with a crude alkyl glycoside inlet (110) in the crude alkyl glycoside fabrication area; the container is equipped with a de-alcoholization pipe (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholization pipe communicates with the crude alkyl glycoside fabrication area, and the lower opening of the de-alcoholization pipe communicates with the gas-liquid separation area inside the de-alcoholizer; the gas-liquid separation area inside the tubular de-alcoholizer is equipped with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104); the de-alcoholization system is equipped with a fatty alcohol condenser (200) for condensing the alcohol vapor generated by the tubular de-alcoholizer into liquid; its characteristic is: The crude alkyl glycoside primary de-alcoholization system includes a gas-liquid separator (600), with the alcohol vapor outlet (104) of the tubular de-alcoholizer entering the inlet of the gas-liquid separator, and the gas phase alcohol outlet (601) of the gas-liquid separator entering the feed inlet of the fatty alcohol condenser.
2. The dealcoholization system according to claim 1, characterized in that... The gas-liquid separator (600) is selected from at least one of the following separators: gas-liquid static separator, centrifugal gas-liquid separator, cyclone gas-liquid separator, filter gas-liquid separator, floating gas-liquid separator, electrostatic precipitator gas-liquid separator, packing separator, and baffle separator.
3. The dealcoholization system according to claim 2, characterized in that... The gas-liquid separator recovers alkyl glycosides from the outlet (603) and inputs them into the tubular dehydrogenator alkyl glycoside material discharge channel (105).
4. The dealcoholization system according to claim 1, characterized in that: An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
5. The dealcoholization system according to claim 1, characterized in that: The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
6. The dealcoholization system according to claim 5, characterized in that: The vacuum buffer tank (300) is equipped with a vacuum interface (302).
7. The dealcoholization system according to claim 5 or 6, characterized in that: The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
8. The dealcoholization system according to claim 7, characterized in that: The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.
9. A primary dealcoholization system for crude alkyl glycosides, comprising a crude alkyl glycoside falling film tubular dealcoholizer (100), the dealcoholizer comprising a container, an upper tube sheet (102) and a lower tube sheet (107) disposed within the container, the container comprising three regions separated by the upper and lower tube sheets, the three regions being a crude alkyl glycoside distribution area, a dealcoholization tube heating area, and a gas-liquid separation area (106) within the dealcoholizer, the crude alkyl glycoside distribution area being located above the upper tube sheet, the dealcoholization tube heating area being located between the upper and lower tube sheets, and the gas-liquid separation area within the dealcoholizer being located below the lower tube sheet; the crude alkyl glycoside distribution area is provided with A crude alkyl glycoside inlet (110) is provided; the container is equipped with a de-alcoholizing pipe (109), which has an upper opening and a lower opening. The upper opening of the de-alcoholizing pipe is connected to the crude alkyl glycoside feeding area, and the upper opening of the de-alcoholizing pipe is higher than the crude alkyl glycoside inlet (110). The lower opening of the de-alcoholizing pipe is connected to the gas-liquid separation zone inside the de-alcoholizer; the gas-liquid separation zone inside the tubular de-alcoholizer is equipped with a tubular de-alcoholizer alkyl glycoside material discharge channel (105) and a tubular de-alcoholizer alcohol vapor outlet (104); the de-alcoholizing system is equipped with a fatty alcohol condenser (200) for condensing the alcohol vapor generated by the tubular de-alcoholizer into liquid; its characteristic is: An internal component (112) is provided at the opening of the deethanolating tube. The internal component (112) extends into the deethanolating tube from the opening. The side of the internal component has the shape of a rotating body side. The top diameter of the rotating body is smaller than the bottom diameter. The lower edge of the rotating body side has a gap with the inner wall of the deethanolating tube.
10. The dealcoholization system according to claim 9, characterized in that... The rotating body is a cone or a frustum.
11. The dealcoholization system according to claim 9, characterized in that... A gas-liquid separator (600) is installed between the alcohol vapor outlet (104) of the tubular alcohol dehydrogenator and the feed inlet of the fatty alcohol condenser. The alcohol vapor outlet (104) of the tubular alcohol dehydrogenator is fed into the inlet of the gas-liquid separator, and the gas phase alcohol outlet (601) of the gas-liquid separator is fed into the feed inlet of the fatty alcohol condenser.
12. The dealcoholization system according to claim 11, characterized in that... The gas-liquid separator (600) is selected from at least one of the following separators: gas-liquid static separator, centrifugal gas-liquid separator, cyclone gas-liquid separator, filter gas-liquid separator, floating gas-liquid separator, electrostatic precipitator gas-liquid separator, packing separator, and baffle separator.
13. The dealcoholization system according to claim 12, characterized in that... The gas-liquid separator recovers alkyl glycosides from the outlet (603) and inputs them into the tubular dehydrogenator alkyl glycoside material discharge channel (105).
14. The dealcoholization system according to claim 9, characterized in that... The axis of the rotating body coincides with the axis of the deethanolating tube.
15. The dealcoholization system according to claim 9, characterized in that... The angle between the generatrix of the rotating body and the axis of the deethanolination tube is α, where α is greater than 0° and less than 90°.
16. The dealcoholization system according to claim 15, characterized in that... α is 5° to 30°.
17. The dealcoholization system according to claim 9, characterized in that... The bottom of the inner component has an axis line extending from the lower edge of the side of the rotating body toward the centerline of the deethanolination tube and an upward curved surface.
18. The dealcoholization system according to claim 9, characterized in that: An alkyl glycoside discharge pump (500) is installed in the alkyl glycoside material discharge channel (105) of the tubular dehydrogenator.
19. The dealcoholization system according to claim 9, characterized in that: The condenser outlet (202) is fed into the vacuum buffer tank (300) inlet.
20. The dealcoholization system according to claim 19, characterized in that... The vacuum buffer tank (300) is equipped with a vacuum interface (302).
21. The dealcoholization system according to claim 19 or 20, characterized in that... The vacuum buffer tank (300) is equipped with a vacuum buffer tank outlet (301).
22. The dealcoholization system according to claim 21, characterized in that: The vacuum buffer tank outlet (301) is fed into the vacuum buffer tank discharge pump (400) inlet.