Method for producing a polyol-containing composition, composition for producing polyurethane, and system for recovering a polyol-containing composition

Abstract

This technology provides a way to purify polyols from polyurethane decomposition liquid in a simple and short time without requiring large-scale equipment. [Solution] A polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid are supplied to a fluid impactor 300 from separate inlets and collided to recover the polyol-containing composition.

Description

[Technical Field]

[0001] The present invention relates to a method for producing a polyol-containing composition, a composition for producing polyurethane, and a recovery system for a polyol-containing composition. [Background Art]

[0002] Polyurethane foams are widely used as cushioning materials, heat insulating materials, structural materials and the like. In recent years, there has been an increasing demand for recycling and reusing polyurethane foams. Generally, when decomposing a polyurethane foam, an amine or a base is added as a decomposition catalyst. As a result, the amine or base mixes into the subsequent recycled raw material, which may cause reaction problems during the reaction and foaming of the recycled polyurethane foam. Therefore, a purification step for removing the amine or base is required, which causes problems such as complicated processes and increased costs. The following techniques are known as techniques for removing impurities. Patent Document 1 discloses a method of removing impurities from a polyurethane decomposition product by distillation. Patent Document 2 discloses a method in which an acid is added to a polyurethane decomposition product to precipitate a hydrochloride, which is then removed by a filter. Patent Document 3 discloses a method in which a polyurethane decomposition product is reacted with an alkylene oxide to be utilized as a low-molecular-weight polyol. Further, as a known technique, purification by extraction utilizing the difference in polarity between impurities and a target product such as polyol is known. [Prior Art Literature] [Patent Literature]

[0003] [Patent Document 1] Japanese Patent No. 4469808 [Patent Document 2] Japanese Patent No. 4501013 [Patent Document 3] Japanese Patent No. 3265085 [Summary of the Invention] [Problems that the invention aims to solve]

[0004] The method of removing impurities from polyurethane decomposition products by distillation requires large-scale distillation equipment, which inevitably leads to increased costs. In methods involving adding acid to polyurethane decomposition products, the added acid remains in the target product, leading to defects in subsequent reactions. The method of reacting polyurethane decomposition products with alkylene oxides requires high-pressure gas equipment. Purification by extraction is a batch process. During this process, emulsification occurs between the polyol layer and the aqueous layer, so it takes time for the layers to separate. In view of the above-mentioned problems, the present invention aims to provide a technology that allows for the simple and rapid purification of polyols from polyurethane decomposition liquid without requiring large-scale equipment. [Means for solving the problem]

[0005] One aspect of the present invention is a method for producing a polyol-containing composition. This method includes the step of supplying a polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid from separate inlets to a fluid impaction device and causing them to collide to recover the polyol-containing composition. In the manufacturing method according to the above embodiment, the solvent may be water. Also, the diameter of the flow path of the fluid impactor may be 1 mm or less.

[0006] Another aspect of the present invention is a composition for the manufacture of polyurethane. This composition for the manufacture of polyurethane includes a polyol-containing composition obtained by the manufacturing method of any of the above-described aspects.

[0007] A further aspect of the present invention is a polyol-containing composition recovery system. This polyol-containing composition recovery system recovers a polyol-containing composition by supplying a polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid from separate inlets and causing them to collide. [Effects of the Invention]

[0008] According to the present invention, it is possible to provide a technology that allows for the simple and rapid purification of polyols from polyurethane decomposition liquid without requiring large-scale equipment. [Brief explanation of the drawing]

[0009] [Figure 1] Figure 1 is a schematic diagram of a polyol-containing composition recovery system. [Figure 2] Figure 2 is a schematic diagram of the microchannels incorporated into the fluid impactor. [Figure 3] Figure 3 is a schematic diagram of another example of a polyol-containing composition recovery system. [Modes for carrying out the invention]

[0010] Embodiments of the present invention will be described in detail below. In this specification, unless otherwise specified, the notation "a~b" in the description of numerical ranges means a or greater and b or less.

[0011] (Polyol-containing composition recovery system) The polyol-containing composition recovery system according to this embodiment recovers the polyol-containing composition by supplying a polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid from separate inlets and causing them to collide. A more specific configuration of the polyol-containing composition recovery system will be described with reference to Figure 1.

[0012] Figure 1 is a schematic diagram of the polyol-containing composition recovery system 10.

[0013] A polyurethane decomposition solution is stored in a polyurethane decomposition solution storage unit 100. The polyurethane decomposition product is obtained by chemically cleaving urethane bonds in a polyurethane product. There is no limitation on the method for cleaving urethane bonds, and examples include aminolysis, acidolysis, glycolysis, hydrogenolysis, thermal decomposition, and decomposition by high-temperature and high-pressure treatment. The polyurethane decomposition product contains, in addition to the polyol to be purified, impurities such as amines. The polyurethane decomposition solution is supplied via a flow path 102 to a fluid collision device 300 to be described later. The amount of the polyurethane decomposition solution supplied to the fluid collision device 300 can be controlled by a pump 110.

[0014] Further, a solvent is stored in a solvent storage unit 200. The solvent has a property of being separable from the polyurethane decomposition solution. Water is preferably used as the solvent having such a property. The solvent is supplied via a flow path 202 to the fluid collision device 300 to be described later. The amount of the solvent supplied to the fluid collision device 300 can be controlled by a pump 210. An appropriate amount of a weak acid solution such as an oxalic acid aqueous solution may be added to the solvent. This makes it possible to reduce the residual amount of amine in an oil layer to be described later, and consequently improve various physical properties of a foam obtained by using the purified polyol obtained by the method of the present disclosure.

[0015] The fluid collision device 300 has a function of causing collision between fluids supplied from separate inlets. Figure 2 is a schematic diagram of a microchannel 310 incorporated in the fluid collision device 300. The fluid collision device 300 of the present embodiment may be referred to as an integrated microreactor. In the microchannel 310, the channel 102 branches into a branch channel 120, a branch channel 130, and a branch channel 140. Comb-shaped channels 121 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels) are formed on one side of the branch channel 120. On one side and the other side of the branch channel 130, there are respectively provided comb-shaped channels 131 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels) and comb-shaped channels 132 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels). Comb-shaped channels 141 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels) are formed on one side of the branch channel 140. Further, in the microchannel 310, the channel 202 branches into a branch channel 220 and a branch channel 230. On one side and the other side of the branch channel 220, there are respectively provided comb-shaped channels 221 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels) and comb-shaped channels 222 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels). On one side and the other side of the branch channel 230, there are respectively provided comb-shaped channels 231 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels) and comb-shaped channels 232 (in the example of FIG. 3, a comb-shaped channel group consisting of four comb-shaped channels). With the above configuration, the comb-shaped channels 121 and the comb-shaped channels 221 are arranged to face each other, the comb-shaped channels 131 and the comb-shaped channels 222 are arranged to face each other, the comb-shaped channels 132 and the comb-shaped channels 231 are arranged to face each other, and the comb-shaped channels 141 and the comb-shaped channels 232 are arranged to face each other. The inner diameter of each branch channel and each comb-shaped channel is, for example, 0.1 to 0.3 μm. The polyurethane decomposition liquid and solvent collide from each comb-shaped channel toward the front side of the paper via slits (not shown), generating a mixed fluid in which an oil phase containing a polyol-containing composition and a solvent phase (specifically, an aqueous phase) are separated. The mixed fluid generated in the fluid collision device 300 passes through a channel 301 provided inside the fluid collision device 300, then passes through a channel 302 connected to the channel 301 and provided outside the fluid collision device 300, and is supplied to the separation device 400. In this embodiment of the fluid impactor, when expressed as M×N, M represents the number of comb-type channel groups in the flow path for one of the liquids (polyurethane decomposition liquid or solvent), and N represents the number of comb-type channels in that comb-type channel group. In other words, M×N represents the total number of comb-type channels provided for one of the liquids. As the mixed fluid passes through the channel 302, impurities from the oil phase are extracted to the solvent side. As a result, the concentration (purity) of the polyol component in the oil phase increases. On the other hand, solvent-affinity (water-soluble) impurities such as amines are extracted to the solvent side. In the mixed fluid, from the viewpoint of facilitating the concentration of the polyol on the oil phase side, the diameter of the flow path 301 is preferably the same as the diameter of the flow path 302, and is 3 mm or less, 2 mm or less, or 1 mm or less. The material of the flow path 302 is not particularly limited as long as it is a hose-like component, but it may be made of resin (for example, PFA: fluororesin) or metal (for example, SUS).

[0016] The separation device 400 has the function of separating the oil phase and the solvent phase according to their specific gravity. The separation device 400 is, for example, a settler. In addition, the separation device 400 may have any mechanism for discharging the separated oil phase, for example, a separatory funnel may be used.

[0017] The oil phase separated in the separation device 400 is sent to the oil phase storage unit 600, where the oil phase is stored as a polyol-containing composition. The oil phase stored in the oil phase storage section 600 may be supplied to the fluid impactor 300 instead of the polyurethane decomposition liquid described above, and the oil phase and solvent phase may be separated again. This makes it possible to increase the concentration of polyol in the resulting oil phase.

[0018] Meanwhile, the solvent phase separated in the separation device 400 is sent to the solvent phase storage unit 500, where the solvent phase is stored.

[0019] According to the polyol-containing composition recovery system 10 of this embodiment, polyols can be purified from polyurethane decomposition liquid simply and quickly without requiring large-scale equipment. Furthermore, by continuously supplying the polyurethane decomposition liquid to the fluid impactor 300, polyols can be continuously purified from the polyurethane decomposition liquid. Furthermore, since only a solvent (specifically water) is added to the polyurethane decomposition solution during treatment, the influence of subsequent reactions using polyols purified from the polyurethane decomposition solution can be suppressed.

[0020] (Other examples of fluid impactors) The fluid impactor 300 is not limited to the microfluidic device described above. Figure 3 is a schematic diagram of another example of a polyol-containing composition recovery system. In the example shown in Figure 3, the fluid impactor 300 is a so-called Y-mixer, in which the polyurethane decomposition liquid and the solvent collide, producing a mixed fluid in which the oil phase containing the polyol-containing composition and the solvent phase (specifically, the aqueous phase) are separated. The mixed fluid produced in the fluid impactor 300 is supplied to the separation device 400 via a channel 301 provided inside the fluid impactor 300, and then via a channel 302 provided outside the fluid impactor 300 and connected to channel 301. In this case, the diameter (inner diameter) of the flow path 301 is preferably 1 mm or less, more preferably 0.5 mm or less, and even more preferably 0.3 mm or less. Furthermore, from the viewpoint of facilitating the concentration of the polyol on the oil phase side, the diameter of the flow path 302 is preferably 3 mm or less, 2 mm or less, or 1 mm or less.

[0021] (Method for producing polyol-containing compositions) The method for producing a polyol-containing composition according to the embodiment includes the step of supplying a polyurethane decomposition liquid and a solvent to be separated from the polyurethane decomposition liquid to a fluid impaction device from separate inlets and causing them to collide, thereby recovering the polyol-containing composition. The polyurethane decomposition liquid and fluid impactor used in the method for producing the polyol-containing composition according to the embodiment are as described in the polyol-containing composition recovery system. The flow rates of the polyurethane decomposition liquid and solvent supplied to the fluid impactor depend on the capacity of the fluid impactor, but for example, they are 1-1000 mL / min, 5-500 mL / min, and 10-250 mL / min for both. By supplying the polyol-containing composition recovered in the process of recovering the polyol-containing composition to the fluid impactor instead of the polyurethane decomposition liquid described above, the concentration of polyol in the polyol-containing composition can be increased.

[0022] According to the method for producing a polyol-containing composition of this embodiment, a polyol-containing composition can be produced simply and quickly from a polyurethane decomposition solution without requiring large-scale equipment. Furthermore, by continuously supplying the polyurethane decomposition liquid to the fluid impactor 300 described above, polyols can be continuously purified from the polyurethane decomposition liquid. Furthermore, since only a solvent (specifically water) is added to the polyurethane decomposition solution during treatment, the influence of subsequent reactions using polyols purified from the polyurethane decomposition solution can be suppressed.

[0023] (Composition for polyurethane manufacturing) The polyurethane manufacturing composition according to the embodiment includes a polyol-containing composition obtained by the method for producing the polyol-containing composition described above.

[0024] The polyol-containing composition is obtained by adding only a solvent (specifically water) without using acid to decompose the polyurethane, and removing impurities such as amines using the fluid impactor described above. Therefore, when the polyol-containing composition is used as a raw material for polyurethane in a subsequent reaction, for example, unwanted side reactions can be suppressed, and the yield of the target product, polyurethane, can be increased.

[0025] The embodiments of the present invention have been described above, but these are merely examples, and various other configurations can also be adopted. [Examples]

[0026] The present invention will be described below with reference to examples and comparative examples, but the present invention is not limited thereto.

[0027] <Preparation of crude polyols> Preparation of crude polyol A 15 g of diethanolamine was added to a flask and heated to 210°C. 100 g of ether polyol-derived urethane foam (manufactured by Inoac Corporation, product name ECA) was added and heated at 210°C for 8 hours. After cooling to room temperature, the upper layer of the decomposition product obtained by centrifugation was recovered as crude polyol A. The viscosity of the obtained crude polyol A was 1100 mPa·s. In this specification, the viscosity of crude polyol is the viscosity at 25°C measured using a B-type rotational viscometer. Preparation of crude polyol B 250 g of the lower layer of the decomposition product obtained during the preparation of crude polyol A was placed in a flask. Next, 500 g of polyether polyol (number average molecular weight 3000, EO content 8%) was placed in the flask. After heating at 60°C for 2 hours until melted, the mixture was collected in a bottle. After cooling to room temperature, the resulting upper layer was collected as crude polyol B. The viscosity of the obtained crude polyol B was 1000 mPa·s. Preparation of crude polyol C Crude polyol C was prepared in the same manner as crude polyol B, except that the polyether polyol was changed to a polyether polyol with a number-average molecular weight of 3000 and an EO ratio of 0%. The viscosity of the obtained crude polyol C was 850 mPa·s. Preparation of crude polyol D Crude polyol D was prepared in the same manner as crude polyol B, except that the polyether polyol was changed to a polyether polyol with a number-average molecular weight of 5000 and an EO ratio of 0%. The viscosity of the obtained crude polyol D was 1500 mPa·s. Table 1 lists the polyol concentration, water content, amine value, hydroxyl value, and viscosity of crude polyols A to D. [Table 1]

[0028] (Example 1) <Preparation of purified polyols> Using a pump, crude polyol A was flowed at a flow rate of 5 mL / min and water at a flow rate of 10 mL / min into a fluid impinger (Mac Engineering Co., Ltd., comb-type integrated microreactor 4x4, internal flow channel diameter 0.2 mm). The mixture stirred in the fluid impinger was passed through a PFA (fluoropolymer) hose with a diameter of φ=2 mm and a length of 10 m. The mixture discharged from the hose was collected in a beaker, with the lower layer (oil phase) being used as the purified polyol and the upper layer as the solvent phase. In Example 1, the time required to obtain purified polyol from 30 mL of crude polyol A (treatment time) was 8 minutes.

[0029] (Example 2) A purified polyol was obtained in the same manner as in Example 1, except that the purified polyol prepared in Example 1 was passed through a fluid impactor instead of the crude polyol A used in Example 1. The time required to obtain the purified polyol from 30 mL of the purified polyol prepared in Example 1 (treatment time) was 8 minutes.

[0030] (Comparative Example 1) 30 mL of crude polyol A and 60 mL of water were added to a separatory funnel and stirred well for 3 minutes. After standing the funnel upright on a separatory funnel stand, the lower layer (oil phase) after 1 hour was used as the purified polyol, and the upper layer was used as the solvent phase. The time required to obtain purified polyol from 30 mL of crude polyol A (treatment time) was 60 minutes.

[0031] (Comparative Example 2) Purified polyol was obtained in the same manner as in Comparative Example 1, except that the standing time was changed to 24 hours. The time required to obtain purified polyol from 30 mL of crude polyol A (treatment time) was 1440 minutes.

[0032] (Evaluation of purified polyols) The obtained purified polyols were dried under reduced pressure at 70°C for 18 hours and then evaluated according to the method described below. The evaluation results are shown in Table 1. (1) Measurement of polyol concentration Polyol concentrations were measured by gel permeation chromatography (GPC). The GPC instrument and measurement conditions used are as follows: GPC equipment: HLC-8320GPC ECOSEC, manufactured by Tosoh Corporation. Column used: TSKgel SuperMultipore HZ-N Mobile phase: THF Flow rate: 1.0mL / min Sample concentration: 0.5% (2) Measurement of amine value The amine values ​​of each example and comparative example were measured in accordance with JIS K1557-7. (3) Hydroxyl value The hydroxyl value of each example and comparative example was measured in accordance with JIS K1557-1, and the obtained hydroxyl value measurements were corrected using the following formula to obtain the corrected hydroxyl value.

number

[0033] [Table 2]

[0034] (Examples 3-7) Crude polyol B was used instead of crude polyol A in Example 1, and the flow velocities of the polyol and water were as shown in Table 3. A comb-type integrated microreactor 8×8 (with a channel diameter of 0.2 mm) manufactured by Mac Engineering was used as the fluid impinger, and the mixed liquid stirred in the fluid impinger was passed through a PFA (fluoropolymer) hose with a diameter of φ=4 mm and a length of 2.5 m. The resulting mixed liquid was collected and analyzed as in Example 1. The results are shown in Table 3. The treatment time in Table 3 is the time required to treat 1 L of polyol.

[0035] [Table 3]

[0036] (Examples 8 and 9) The experiment was conducted in the same manner as in Example 1, except that crude polyol C was used instead of crude polyol A, and the flow rates of polyol and water were as shown in Table 4. The results obtained are shown in Table 4. The treatment time in Table 4 is the time required for treatment with 30 mL of polyol.

[0037] (Examples 10, 11) The experiment was conducted in the same manner as in Example 1, except that crude polyol D was used instead of crude polyol A, and the flow rates of polyol and water were as shown in Table 4. The results obtained are shown in Table 4. The treatment time in Table 4 is the time required for treatment with 30 mL of polyol.

[0038] [Table 4]

[0039] (Evaluation when using an aqueous oxalic acid solution as the solvent) (Example 12) Using a pump, the crude polyol B described above was flowed at a flow rate of 5 mL / min and a 0.1 M oxalic acid aqueous solution at a flow rate of 10 mL / min through a comb-shaped, integrated microreactor 4x4 manufactured by Mac Engineering. The mixture stirred in the integrated microreactor 4x4 was passed through a hose with a diameter of φ=2.0 mm and a length of 10 m. The mixture discharged from the hose was collected in a beaker. Using a pump, the lower layer collected in the beaker was flowed again through the comb-shaped integrated microreactor 4x4 at a flow rate of 5 mL / min and water at a flow rate of 10 mL / min. The mixture stirred in the integrated microreactor 4x4 was passed through a hose with a diameter of φ=2.0 mm and a length of 10 m made of PFA. The mixture discharged from the hose was collected in a beaker, with the lower layer (oil phase) being used as the purified polyol and the upper layer as the solvent phase.

[0040] (Example 13) A purified polyol was obtained in the same manner as in Example 12, except that a 0.3 M aqueous solution of oxalic acid was used instead of the 0.1 M aqueous solution of oxalic acid used in Example 12.

[0041] (Example 14) A purified polyol was obtained in the same manner as in Example 12, except that water was used instead of the 0.1 M oxalic acid aqueous solution used in Example 12.

[0042] For the purified polyols of Examples 12, 13, and 14, the polyol concentration, amine value, and hydroxyl value were measured in accordance with the (Evaluation of Purified Polyols) described above. The peak of C=O derived from oxalic acid (1720CM) was detected by FT-IR. -1 Based on the presence or absence of (nearby) oxalic acid residue, no oxalic acid residue was found in Examples 12 and 13. Table 5 shows the polyol concentration, water content, amine value, hydroxyl value, and viscosity of the purified polyols from Examples 12, 13, and 14.

[0043] [Table 5]

[0044] (Foaming using purified polyols) Polyurethane raw materials were prepared based on the formulations listed in Table 6, foamed, and then heated at 70°C for 1 hour to obtain a polyurethane foam. The details of the raw materials listed in Table 6 are as follows: Polyol a: Number average molecular weight 3000, number of functional groups 3, hydroxyl value (OHV) 56.1 mgKOH / g, EO% = 8%, product code: GP3050NS, manufactured by Sanyo Chemical Industries, Ltd. Crude polyol: Crude polyol B Purified polyol a: Purified polyol prepared in Example 14, Purified polyol b: Purified polyol prepared in Example 12 Purified polyol c: Purified polyol prepared in Example 13 Amine catalyst: N,N-dimethylaminohexanol, product number: Kaolizer No. 25, manufactured by Kao Corporation. Foam stabilizer: Silicone foam stabilizer, part number: NIAX L-895, manufactured by Momentive Performance Materials, Inc.; Metal catalyst: Dibutyltin dilaurate, part number: MRH-110, manufactured by Johoku Chemical Industry Co., Ltd. Isocyanate: TDI, NCO %=48.2%, Product code: Cosmonate T-80, manufactured by Mitsui Chemicals, Inc.

[0045] <Recycling rate> The recycling rate for foaming, as shown in Table 6, was calculated according to the following formula.

number

[0046] <Amine value> The amine value of the entire polyol component was calculated according to the following formula.

number

[0047] <CT(クリームタイム)> The time it took for the prepared composition to begin foaming and for the liquid level to rise (begin to expand) was measured as the cream time (CT).

[0048] <RT(ライズタイム)> The time from when the prepared composition began to foam until the change in foam height completely stopped was measured as RT (rise time).

[0049] <Apparent Density> The apparent density of the obtained foam is (kg / m³ 3 The values ​​were measured in accordance with JIS K 7222.

[0050] <Tensile strength, elongation, and tear strength> The tensile strength (kPa), elongation (%), and tear strength (N / cm) of the obtained foam were measured in accordance with JIS K 6400-5.

[0051] [Table 6]

[0052] Formula 1, which serves as the basis for each formulation listed in Table 6, is a foam formulation using only polyol a as the polyol component. Formulas 2 and 3 are recycled foam formulations using crude polyol. It can be seen that a decrease in physical properties occurs as the recycling rate increases. In particular, the decrease in physical properties was more pronounced in Formula 3 than in Formula 1, suggesting that it is difficult to further increase the recycling rate. Formulations 4 and later utilize a foam formulation with purified polyol. It was shown that a lower amine value of the purified polyol leads to a higher recycling rate. [Industrial applicability]

[0053] According to the method for producing a polyol-containing composition or the polyol-containing composition recovery system of this disclosure, high-purity polyols can be easily recovered from polyurethane foams, which is useful for recycling polyurethane foams. [Explanation of symbols]

[0054] 10 Polyol-containing composition recovery system, 100 Polyurethane decomposition liquid storage section, 102 Flow channel, 110 Pump, 120 Branching flow channel, 121 Comb-shaped flow channel, 130 Branching flow channel, 131, Comb-shaped flow channel, 132 Comb-shaped flow channel, 140 Branching flow channel, 141 Comb-shaped flow channel, 300 Fluid impactor, 200 Solvent storage section, 202 Flow channel, 210 Pump, 220 Branching flow channel, 221 Comb-shaped flow channel, 222 Comb-shaped flow channel, 230 Branching flow channel, 231 Comb-shaped flow channel, 232 Comb-shaped flow channel, 301 Flow channel, 302 Flow channel, 310 Microflow channel, 400 Separation device, 500 Solvent phase storage section, 600 Oil phase storage section

Claims

1. A method for producing a polyol-containing composition, comprising the step of supplying a polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid to a fluid impactor from separate inlets and causing them to collide to recover the polyol-containing composition.

2. The manufacturing method according to claim 1, wherein the solvent is water.

3. The manufacturing method according to claim 1, wherein the diameter of the flow path of the fluid impactor is 1 mm or less.

4. A composition for producing polyurethane, comprising a polyol-containing composition obtained by the manufacturing method described in any one of claims 1 to 3.

5. A polyol-containing composition recovery system that recovers a polyol-containing composition by supplying a polyurethane decomposition liquid and a solvent for separating the polyurethane decomposition liquid from separate inlets and causing them to collide.

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