Production method of 1, 2-pentanediol

Abstract

The present invention relates to the technical field of pentanediol production, particularly to a 1, 2-pentanediol production method, which comprises that a furfuryl alcohol-containing reaction liquid is subjected to a hydrogenation reaction under the action of a hydrogenation catalyst to generate 1, 2-pentanediol, the base number of the reaction liquid is 100-500 ppm, and the hydrogenation catalyst comprises 50-70 wt% of CuO, 10-30 wt% of ZnO, 5-10 wt% of 1, 2-pentanediol, and 5-10 wt% of 1, 2-pentanediol according to the total mass of the hydrogenation catalyst. The component A comprises, by weight, 35%-20% of Al2O3 and 2%-10% of La2O3; according to the hydrogenation catalyst with the specific composition and proportion, the selectivity of 1, 2-pentanediol can be obviously improved, side reactions are reduced, the side reactions are also obviously reduced by controlling the base number of a reaction solution to be within the range, especially the content of valerolactone in a crude product is reduced, so that the separation difficulty of the product is simplified, the purity of the product is obviously improved, and the production cost is reduced. The product quality is ensured. The obtained product has no peculiar smell, can be applied to the field of cosmetics, and belongs to cosmetic-grade 1, 2-pentanediol.

Description

Technical Field

[0001] The present invention relates to the technical field of pentanediol production, and in particular to a method for producing 1,2-pentanediol. Background Art

[0002] 1,2-Pentanediol (i.e. 1,2-PeD) is an important high-value-added chemical, mainly used in the production of polyester fibers, various cosmetics and skin care products, surfactants, disinfectants, printing inks, emulsifiers, plasticizers, medical supplies, etc. It is also an important intermediate for the synthesis of the fungicide propiconazole.

[0003] The main synthetic routes for 1,2-pentanediol currently include the epoxidation-hydrolysis method for 1-pentene and the cyanation-esterification-hydrogenation method for n-butyraldehyde. The epoxidation-hydrolysis method for 1-pentene involves hydrogen peroxide epoxidation, which is a dangerous process and produces a large amount of wastewater. The cyanation-esterification-hydrogenation method for n-butyraldehyde involves the use of the highly toxic chemical hydrocyanic acid, which is also a dangerous process and produces a large amount of saline wastewater as a by-product. Furthermore, the product's odor verification cannot be used in the downstream cosmetics industry.

[0004] The one-step catalytic hydrogenation of furfuryl alcohol to produce 1,2-pentanediol has an efficient reaction process, a simple purification process, and low investment, making it more suitable for industrial-scale production. The key to the furfuryl alcohol hydrogenation method lies in the development of suitable efficient catalysts and production processes.

[0005] Patents CN201911107004.9 and CN201320723632.6 both report methods for producing 1,2-pentanediol by hydrogenolysis of furfuryl alcohol using precious metal catalysts. However, the maximum yield of 1,2-pentanediol in the product is only approximately 40%, and the high catalyst cost of this process makes it difficult to industrialize. Patent CN116920854 discloses a method for preparing a catalyst and a method for selectively hydrogenating furfuryl alcohol to produce 1,2-pentanediol using the catalyst. However, the selectivity for 1,2-pentanediol is low, and the product produces a large number of byproducts, particularly the key impurity valerolactone, which is difficult to separate from the main product, making it difficult to apply in downstream cosmetics.

[0006] How to develop efficient non-precious metal catalysts to improve the selectivity of 1,2-pentanediol while controlling the content of key impurities to ensure product quality is the key to the industrialization of furfuryl alcohol hydrogenation to produce 1,2-pentanediol. Summary of the Invention

[0007] Therefore, the technical problem to be solved by the present invention is to overcome the defects of the prior art of preparing 1,2-pentanediol by hydrogenation of furfuryl alcohol, such as low selectivity resulting in a large number of by-products and difficulty in product separation resulting in an increased content of key impurities in the pure product, thereby providing a method for producing 1,2-pentanediol.

[0008] The present application provides a method for producing 1,2-pentanediol, comprising: subjecting a reaction solution containing furfuryl alcohol to a hydrogenation reaction under the action of a hydrogenation catalyst to generate 1,2-pentanediol, wherein the reaction solution has an alkali value of 100-500 ppm, and the hydrogenation catalyst comprises 50 wt%-70 wt% of CuO, 10 wt%-30 wt% of ZnO, 5 wt%-20 wt% of Al2O3, and 2 wt%-10 wt% of La2O3, based on the total mass of the hydrogenation catalyst.

[0009] Furthermore, based on the total mass of the hydrogenation catalyst, the hydrogenation catalyst comprises 58 wt%-62 wt% of CuO, 18 wt%-22 wt% of ZnO, 12 wt%-16 wt% of Al2O3 and 4 wt%-6 wt% of La2O3.

[0010] Furthermore, based on the total mass of the hydrogenation catalyst, the hydrogenation catalyst includes 60 wt% of CuO, 20 wt% of ZnO, 15 wt% of Al2O3 and 35 wt% of La2O.

[0011] Furthermore, the alkali value of the reaction solution is 200-300 ppm.

[0012] Furthermore, the alkalinity of the reaction solution is controlled by adding an inorganic base or an organic base to the reaction solution;

[0013] Optionally, the inorganic base is selected from one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, potassium carbonate, sodium bicarbonate, and potassium bicarbonate;

[0014] Optionally, the organic base is selected from one or more of tetramethylammonium hydroxide, triethylamine, sodium methoxide, potassium ethoxide, and potassium tert-butoxide.

[0015] In some embodiments, an aqueous solution of an inorganic base or an organic base (such as a sodium carbonate solution or a tetramethylammonium hydroxide solution) may be added, and the mass percentage of the solution is 0.5-10 wt%, for example, 0.5 wt%, 1 wt%, 5 wt% or 10 wt%.

[0016] Furthermore, the solvent of the reaction solution is selected from one or more of alcohol solvents (e.g., C1-C20 alcohol solvents), amide solvents (C1-C20 amide solvents), and alkane solvents (C1-C15 alkane solvents); preferably, an alcohol solvent; more preferably, methanol or ethanol.

[0017] Furthermore, the reaction pressure of the hydrogenation reaction is 2-10 MPa, preferably 4-8 MPa.

[0018] Furthermore, the reaction temperature of the hydrogenation reaction is 120-250°C, preferably 130-180°C.

[0019] Furthermore, the preparation method of the hydrogenation catalyst comprises the following steps:

[0020] The metal salt solution containing copper salt, zinc salt, aluminum salt and lanthanum salt is mixed with the precipitant solution, reacted, allowed to stand for aging, solid-liquid separation, and the precipitate is dried and calcined to obtain the hydrogenation catalyst;

[0021] Optionally, the reaction temperature is 40-80°C;

[0022] Optionally, the pH value of the reaction system is 6.5-8;

[0023] Optionally, the static aging time is 0.5-3h;

[0024] Optionally, the drying temperature is 100-200° C. and the drying time is 5-10 hours;

[0025] Optionally, the moisture content of the precipitate after drying is 1-5 wt%;

[0026] Optionally, the calcination temperature is 300-600° C. and the calcination time is 2-5 h;

[0027] Optionally, the copper salt is selected from one or more of copper nitrate and copper chloride; and / or the zinc salt is selected from one or more of zinc nitrate and zinc chloride; and / or the aluminum salt is selected from one or more of aluminum nitrate and aluminum chloride; and / or the lanthanum salt is selected from one or more of lanthanum nitrate and lanthanum chloride; and / or the precipitant is selected from one or more of sodium carbonate, potassium carbonate, sodium hydroxide, potassium hydroxide, ammonium carbonate or ammonia water.

[0028] Furthermore, the mass space velocity of furfuryl alcohol during the hydrogenation reaction was 0.1h -1 -0.5h -1 .

[0029] Furthermore, during the hydrogenation reaction, the molar ratio of hydrogen to furfuryl alcohol is 30-100:1, preferably 50:1.

[0030] Furthermore, the hydrogenation catalyst undergoes a hydrogenation reaction in a mixed atmosphere of nitrogen and hydrogen.

[0031] The volume ratio of nitrogen to hydrogen in the mixed atmosphere is 75-85:20.

[0032] Furthermore, before the hydrogenation reaction, the method further includes a step of reducing and activating the hydrogenation catalyst in a mixed atmosphere of nitrogen and hydrogen.

[0033] During the reduction activation process, the volume ratio of nitrogen to hydrogen is 90-95:5, and the temperature of the reduction activation is 120-170°C.

[0034] Furthermore, the 1,2-pentanediol production method may further include a step of purifying the crude product after the hydrogenation reaction. This application does not limit the purification method, and purification can be performed using conventional methods in the art, such as distillation. For example, the number of plates may be 40-60, the top pressure may be 1-2.5 kPaA, the top temperature may be 125-135°C, and the reflux ratio may be 8-12:1.

[0035] Furthermore, a trickle bed or a bubbling bed is used for the hydrogenation reaction, preferably a trickle bed is used for the hydrogenation reaction.

[0036] Furthermore, in the hydrogenation reaction, the furfuryl alcohol conversion rate is ≥99.2%, the 1,2-pentanediol selectivity is ≥78%, the valerolactone content in the crude 1,2-pentanediol is <500 ppm, the purity of the pure 1,2-pentanediol is >99.9%, and the valerolactone content in the pure 1,2-pentanediol is <200 ppm.

[0037] Optionally, in the hydrogenation reaction, the furfuryl alcohol conversion rate is 99.2%-99.7%, the 1,2-pentanediol selectivity is 78%-85%, the valerolactone content in the crude 1,2-pentanediol is <500 ppm (e.g., 300 ppm-480 ppm), the purity of pure 1,2-pentanediol is 99.9-99.96%, and the valerolactone content of pure 1,2-pentanediol is <200 ppm (e.g., 100-168 ppm).

[0038] The technical solution of the present invention has the following advantages:

[0039] 1. The present invention provides a method for producing 1,2-pentanediol, comprising hydrogenating a reaction solution containing furfuryl alcohol in the presence of a hydrogenation catalyst to produce 1,2-pentanediol. The reaction solution has an alkalinity of 100-500 ppm, and the hydrogenation catalyst comprises, based on the total mass of the hydrogenation catalyst, 50-70 wt% CuO, 10-30 wt% ZnO, 5-20 wt% Al2O3, and 2-10 wt% La2O3. The hydrogenation catalyst having the above-specified composition and ratio significantly improves the selectivity of 1,2-pentanediol and reduces the occurrence of side reactions. Controlling the alkalinity of the reaction solution within the above-specified range also significantly reduces the occurrence of side reactions, particularly reducing the content of valerolactone in the crude product, thereby simplifying product separation, significantly improving product purity, and ensuring product quality. The resulting product is odorless and can be used in cosmetics, representing cosmetic-grade 1,2-pentanediol.

[0040] 2. The present invention provides a method for producing 1,2-pentanediol. The hydrogenation catalyst comprises, based on the total mass of the hydrogenation catalyst, 58-62 wt% CuO, 18-22 wt% ZnO, 12-16 wt% Al2O3, and 4-6 wt% La2O3. By controlling the contents of each substance in the hydrogenation catalyst within the aforementioned ranges, the conversion of furfuryl alcohol and the selectivity for 1,2-pentanediol can be further improved, the occurrence of side reactions can be further reduced, and the product purity can be improved.

[0041] 3. In the method for producing 1,2-pentanediol provided by the present invention, the alkalinity of the reaction solution is 200-300 ppm. By controlling the alkalinity of the reaction solution within the above range, the conversion rate of furfuryl alcohol and the selectivity of 1,2-pentanediol can be further improved, and the occurrence of side reactions can be further reduced, thereby improving product purity. DETAILED DESCRIPTION

[0042] The following examples are provided for a better understanding of the present invention and are not intended to limit the best mode of implementation. They do not limit the content and scope of protection of the present invention. Any product identical or similar to the present invention obtained by anyone under the guidance of the present invention or by combining the features of the present invention with other prior arts shall fall within the scope of protection of the present invention.

[0043] If specific experimental procedures or conditions are not specified in the examples, the procedures or conditions described in the literature in the field can be followed. Reagents or instruments used without manufacturer's indication are commercially available conventional reagents. V / V represents the volume ratio.

[0044] The reagents and solvents used in the present invention can be purchased from Aladdin Reagent Company.

[0045] Catalyst performance evaluation was performed using a Shimadzu GC-2010 gas chromatograph (with a hydrogen flame detector and nitrogen as carrier gas). The instrument was equipped with a DB-5 capillary column (5% phenylmethylsiloxane as the stationary phase, 30 m × 0.32 mm × 0.25 μm) and a hydrogen flame detector (FID). Both the injector and detector temperatures were 280°C. The column temperature was programmed: initially at 100°C for 0.5 minutes, then increased at 15°C / min to 260°C and held for 5 minutes. The column pressure was 8.5868 psi (approximately 59.2 kPa), and the flow rate was 1.5 mL / min. The injection volume was 0.2 μL. Conversion and selectivity were calculated using the area normalization method. The purity of pure 1,2-pentanediol and the valerolactone content in crude or pure 1,2-pentanediol were also calculated using the area normalization method.

[0046] Example 1

[0047] This embodiment provides a method for producing 1,2-pentanediol, comprising the following steps:

[0048] 100 g of hydrogenation catalyst was loaded into a trickle bed reactor, and the hydrogenation catalyst was reduced and activated in an atmosphere of nitrogen: hydrogen = 95:5 (V / V). The activation temperature was 150° C., and the temperature rise was controlled not to exceed 20° C. After the catalyst bed had no temperature rise, the volume ratio of nitrogen: hydrogen was adjusted to 80:20 (V / V), and the temperature was kept at 150° C. for 24 h. The reaction liquid (i.e., an ethanol solution containing 20% by mass of furfuryl alcohol) was continuously introduced into the reactor. The reaction pressure was controlled to 6 MPa, the temperature was 150° C., and the mass space velocity of furfuryl alcohol was 0.2 h -1 The molar ratio of hydrogen to furfuryl alcohol was 50:1, and 1 wt% sodium hydroxide solution was added to control the alkalinity of the reaction solution to 200 ppm. After stabilization for 8 hours, samples were collected for analysis. The furfuryl alcohol conversion, 1,2-pentanediol selectivity, and the content of the key byproduct valerolactone are shown in Table 1.

[0049] The crude 1,2-pentanediol obtained by the reaction was distilled with the number of plates controlled at 50, the top pressure at 2 kPaA, the top temperature at 130°C, and the reflux ratio at 10:1 to obtain pure 1,2-pentanediol. The purity of the pure 1,2-pentanediol and the content of the key by-product valerolactone are shown in Table 1.

[0050] The specific preparation method of the hydrogenation catalyst used in this embodiment is as follows: 141.47g of copper nitrate, 46.54g of zinc nitrate, 62.67g of aluminum nitrate, and 9.97g of lanthanum nitrate are dissolved in water and diluted to a constant volume of 1000mL to obtain a mixed solution. 10wt% sodium carbonate solution is added dropwise to the mixed solution to carry out a precipitation reaction, and the pH value of the precipitation reaction is controlled to be 7.5 and the temperature is 60°C. After the reaction is completed, the mixture is allowed to stand for aging for 2 hours, then filtered, washed, dried at 150°C for 8h (water content is 3%), and calcined at 400°C for 3h to obtain the hydrogenation catalyst. Based on the gross mass of the hydrogenation catalyst, the composition of the hydrogenation catalyst is: the content of CuO is 60wt%, the content of ZnO is 20wt%, the content of Al2O3 is 15wt%, and the content of La2O3 is 5wt%.

[0051] Example 2

[0052] This embodiment provides a production method of 1,2-pentanediol, which is basically the same as that of Example 1, except that, in the preparation process of the hydrogenation catalyst, "165.04 g of copper nitrate, 34.91 g of zinc nitrate, 41.78 g of aluminum nitrate, and 9.97 g of lanthanum nitrate are dissolved in water" replaces "141.47 g of copper nitrate, 46.54 g of zinc nitrate, 62.67 g of aluminum nitrate, and 9.97 g of lanthanum nitrate are dissolved in water" in Example 1. The remaining process conditions are the same as those in Example 1. The composition of the obtained hydrogenation catalyst is: the content of CuO is 70 wt%, the content of ZnO is 15 wt%, the content of Al2O3 is 10 wt%, and the content of La2O3 is 5 wt%.

[0053] Example 3

[0054] This embodiment provides a production method of 1,2-pentanediol, which is basically the same as that of Example 1, except that, in the preparation process of the hydrogenation catalyst, "129.68 g of copper nitrate, 58.18 g of zinc nitrate, 71.03 g of aluminum nitrate, and 5.98 g of lanthanum nitrate are dissolved in water" replaces "141.47 g of copper nitrate, 46.54 g of zinc nitrate, 62.67 g of aluminum nitrate, and 9.97 g of lanthanum nitrate are dissolved in water" in Example 1. The remaining process conditions are the same as those in Example 1. The composition of the obtained hydrogenation catalyst is: the content of CuO is 55 wt%, the content of ZnO is 25 wt%, the content of Al2O3 is 17 wt%, and the content of La2O3 is 3 wt%.

[0055] Example 4

[0056] This embodiment provides a method for producing 1,2-pentanediol, comprising the following steps:

[0057] 100 g of hydrogenation catalyst (prepared by the same method as that of the hydrogenation catalyst in Example 1) was loaded into a trickle bed reactor, and the catalyst was reduced and activated in an atmosphere of nitrogen:hydrogen=95:5 (V / V). The activation temperature was 150° C., and the temperature rise was controlled not to exceed 20° C. After the catalyst bed had no temperature rise, the volume ratio of nitrogen:hydrogen was adjusted to 80:20 (V / V), and the temperature was kept at 150° C. for 24 h. The reaction liquid (i.e., an ethanol solution containing 20% furfuryl alcohol) was continuously introduced into the reactor, and the reaction pressure was controlled to 5 MPa, the temperature was 160° C., and the mass space velocity of furfuryl alcohol was 0.1 h -1 The hydrogen-to-furfuryl alcohol molar ratio was 50:1, and a 10 wt% tetramethylammonium hydroxide solution was added to control the reaction mixture's alkalinity to 250 ppm. After stabilization for 8 hours, samples were collected for analysis. The furfuryl alcohol conversion, 1,2-pentanediol selectivity, and the content of the key byproduct valerolactone are shown in Table 1.

[0058] The crude 1,2-pentanediol obtained by the reaction was distilled with the number of plates controlled at 50, the top pressure at 2 kPaA, the top temperature at 130°C, and the reflux ratio at 10:1 to obtain pure 1,2-pentanediol. The purity of the pure 1,2-pentanediol and the content of the key by-product valerolactone are shown in Table 1.

[0059] Example 5

[0060] This embodiment provides a method for producing 1,2-pentanediol, which is basically the same as Example 1, except that the alkalinity of the reaction solution is controlled differently during the hydrogenation reaction. In this embodiment, a 1 wt % sodium hydroxide solution is used to control the alkalinity of the reaction solution to 500 ppm.

[0061] Example 6

[0062] This embodiment provides a method for producing 1,2-pentanediol, which is basically the same as Example 1, except that the alkalinity of the reaction solution is controlled differently during the hydrogenation reaction. In this embodiment, a 1 wt % sodium hydroxide solution is used to control the alkalinity of the reaction solution to 100 ppm.

[0063] Example 7

[0064] This embodiment provides a method for producing 1,2-pentanediol, which is basically the same as that of Example 1, except that the reaction liquid solvent is different. This embodiment uses "N,N-dimethylformamide solution containing 20% by mass of furfuryl alcohol" instead of "ethanol solution containing 20% by mass of furfuryl alcohol" in Example 1.

[0065] Example 8

[0066] This embodiment provides a method for producing 1,2-pentanediol, which is basically the same as that of Example 1, except that the aging time during the preparation of the hydrogenation catalyst is different. The aging time in this embodiment is 0.5 h.

[0067] Comparative Example 1

[0068] This comparative example provides a production method of 1,2-pentanediol, which is basically the same as that of Example 1, except that, in the preparation process of the hydrogenation catalyst, "153.25 g of copper nitrate, 46.54 g of zinc nitrate, 65.67 g of aluminum nitrate, and 0 g of lanthanum nitrate are dissolved in water" replaces "141.47 g of copper nitrate, 46.54 g of zinc nitrate, 62.67 g of aluminum nitrate, and 9.97 g of lanthanum nitrate are dissolved in water" in Example 1, and the remaining process conditions are the same as those in Example 1. The composition of the obtained hydrogenation catalyst is: the content of CuO is 65 wt%, the content of ZnO is 20 wt%, the content of Al2O3 is 15 wt%, and the content of La2O3 is 0 wt%.

[0069] Comparative Example 2

[0070] This embodiment provides a method for producing 1,2-pentanediol, which is basically the same as that of Example 1, except that no sodium hydroxide solution is added to the reaction solution during the hydrogenation reaction, and the alkalinity of the reaction solution is monitored to be less than 5 ppm.

[0071] The experimental results of each embodiment and comparative example are shown in Table 1.

[0072] Table 1 Experimental results

[0073]

[0074] The test results of the above embodiments and comparative examples show that, compared with Comparative Examples 1-2, the present invention adopts the methods of each embodiment to prepare cosmetic-grade 1,2-pentanediol, which significantly improves the furfuryl alcohol conversion rate (≥99.2%) and 1,2-pentanediol selectivity (≥78%), and greatly reduces the content of by-products, wherein the content of the key impurity valerolactone is less than 500 ppm, the separation difficulty is small, and the purity of the pure product after distillation is significantly improved (purity>99.9%, valerolactone content <200 ppm). It also has the significant advantages of simple operation and easy industrialization, no odor, and can be used in the field of cosmetics.

[0075] Obviously, the above embodiments are merely examples for clarity of explanation and are not intended to limit the implementation methods. Those skilled in the art will readily appreciate that other variations or modifications based on the above descriptions are possible. It is not necessary and impossible to enumerate all implementation methods here. Obvious variations or modifications arising therefrom remain within the scope of protection of the present invention.

Claims

1. A method for producing 1,2-pentanediol, characterized in that: The method comprises the following steps: subjecting a reaction liquid containing furfuryl alcohol to a hydrogenation reaction under the action of a hydrogenation catalyst to generate 1,2-pentanediol, wherein the alkali value of the reaction liquid is 100-500 ppm, and based on the total mass of the hydrogenation catalyst, the hydrogenation catalyst comprises 50wt%-70wt% of CuO, 10wt%-30wt% of ZnO, 35wt%-20wt% of Al2O, and 32wt%-10wt% of La2O.

2. The production method according to claim 1, characterized in that Based on the total mass of the hydrogenation catalyst, the hydrogenation catalyst comprises 58wt%-62wt% of CuO, 18wt%-22wt% of ZnO, 12wt%-16wt% of Al2O3 and 4wt%-6wt% of La2O3.

3. The production method according to claim 1 or 2, characterized in that The alkali value of the reaction solution is 200-300 ppm.

4. The production method according to any one of claims 1 to 3, characterized in that controlling the alkalinity of the reaction solution by adding an inorganic base or an organic base to the reaction solution; Optionally, the inorganic base is selected from one or more of sodium hydroxide, potassium hydroxide, sodium carbonate, potassium carbonate, sodium bicarbonate, and potassium bicarbonate; Optionally, the organic base is selected from one or more of tetramethylammonium hydroxide, triethylamine, sodium methoxide, potassium ethoxide, and potassium tert-butoxide.

5. The production method according to any one of claims 1 to 4, characterized in that The solvent of the reaction solution is selected from one or more of alcohol solvents, amide solvents, and alkane solvents; preferably, an alcohol solvent; more preferably, methanol or ethanol.

6. The production method according to any one of claims 1 to 5, characterized in that The reaction pressure of the hydrogenation reaction is 2-10 MPa, preferably 4-8 MPa.

7. The production method according to any one of claims 1 to 6, characterized in that The reaction temperature of the hydrogenation reaction is 120-250°C, preferably 130-180°C.

8. The production method according to any one of claims 1 to 7, characterized in that The preparation method of the hydrogenation catalyst comprises the following steps: The metal salt solution containing copper salt, zinc salt, aluminum salt and lanthanum salt is mixed with the precipitant solution, reacted, allowed to stand for aging, solid-liquid separation, and the precipitate is dried and calcined to obtain the hydrogenation catalyst; Optionally, the reaction temperature is 40-80°C; Optionally, the pH value of the reaction system is 6.5-8; Optionally, the static aging time is 0.5-3h; Optionally, the drying temperature is 100-200° C. and the drying time is 5-10 hours; Optionally, the moisture content of the precipitate after drying is 1-5 wt%; Optionally, the calcination temperature is 300-600° C. and the calcination time is 2-5 h; Optionally, the copper salt is selected from one or more of copper nitrate and copper chloride; and / or the zinc salt is selected from one or more of zinc nitrate and zinc chloride; and / or the aluminum salt is selected from one or more of aluminum nitrate and aluminum chloride; and / or the lanthanum salt is selected from one or more of lanthanum nitrate and lanthanum chloride; and / or the precipitant is selected from one or more of sodium carbonate, potassium carbonate, sodium hydroxide, potassium hydroxide, ammonium carbonate or ammonia water.

9. The production method according to any one of claims 1 to 8, characterized in that The hydrogenation reaction is carried out using a trickle bed or a bubbling bed; and / or, the hydrogenation reaction further comprises a step of purifying the crude product; and / or, the mass space velocity of furfuryl alcohol during the hydrogenation reaction is 0.1h -1 -0.5h -1 ; and / or, the molar ratio of hydrogen to furfuryl alcohol during the hydrogenation reaction is 30-100:

1.

10. The production method according to any one of claims 1 to 9, characterized in that: In the hydrogenation reaction, the furfuryl alcohol conversion rate is ≥99.2%, the 1,2-pentanediol selectivity is ≥78%, the valerolactone content in the crude 1,2-pentanediol is <500 ppm, the purity of the pure 1,2-pentanediol is >99.9%, and the valerolactone content in the pure 1,2-pentanediol is <200 ppm; optionally, in the hydrogenation reaction, the furfuryl alcohol conversion rate is 99.2%-99.7%, the 1,2-pentanediol selectivity is 78%-85%, the valerolactone content in the crude 1,2-pentanediol is <500 ppm, the purity of the pure 1,2-pentanediol is 99.9-99.96%, and the valerolactone content in the pure 1,2-pentanediol is <200 ppm.

Images