Production process of solubilizer and refrigerating machine oil containing solubilizer

Abstract

The invention discloses a production process of a solubilizer and refrigerating machine oil containing the solubilizer. Introducing naphtha into an ion exchange membrane filter to obtain impurity-removed naphtha; the oil enters a preheater and is heated to 40-55 DEG C, and preheated oil is obtained; flowing into a fractionating tower to cut fractions with the distillation range of 60-170 DEG C to obtain distillate oil; entering a polymerization reactor to finish a polymerization reaction to obtain polymerized oil; entering a light hydrogenation reactor, and carrying out a light hydrogenation reaction under the action of a catalyst to obtain refined oil; further fractionating in a rectifying tower, wherein the extracted fraction with the distillation range of 180-205 DEG C is the solubilizer; and after being condensed by the condenser, the solubilizer flows into the solubilizer storage tank or is pumped into the refrigerating machine oil production unit. According to the production process, the production process route of the solubilizer is widened, and the production efficiency is improved. According to the refrigerating machine oil containing the solubilizer, the solubility at a low temperature and the intersolubility with a refrigerant are improved, and the precipitation phenomenon at the low temperature is weakened, so that the performance and the quality of the refrigerating machine oil are improved.

Description

Technical Field

[0001] The invention relates to the field of refrigerator lubricants, in particular to a production process of a solubilizer and refrigerator oil containing the solubilizer. Background Art

[0002] Refrigeration oil is a lubricant mainly used in refrigeration equipment. It plays a key role in the function and effect of the refrigeration system, especially in lubrication, cooling, sealing and reducing machine noise. In order to ensure the normal operation of related dynamic equipment and the system in which it is located, the refrigeration oil needs to have good chemical stability when coexisting with the refrigerant, excellent miscibility with the refrigerant, good lubricity, excellent low-temperature fluidity, no waxy flocculent separation, no water, no mechanical impurities and excellent insulation performance.

[0003] In addition to the various properties mentioned above, the characteristics of refrigeration oil also need to pay attention to its appearance. Qualified refrigeration oil should be a transparent liquid without impurities. If the color deepens or becomes white or turbid during use, it means that the refrigeration oil has deteriorated and needs to be replaced in time.

[0004] Therefore, refrigeration oil can effectively lubricate and cool the various components of the refrigeration system, thereby improving the operating efficiency and stability of the entire system. However, its disadvantages include high prices and the need for regular replacement.

[0005] In terms of the operating process, the refrigeration compressor relies on the reduced pressure evaporation of the refrigerant to achieve low temperature during the working process, while the refrigeration oil lubricates the working parts of the refrigeration system.

[0006] As for the current development status, in recent years, the technology of various refrigeration devices such as refrigerators, freezers, air conditioners, large cold storages, refrigerated trucks, etc. has been increasingly improved. Power saving, rotation, small and light weight, full enclosure and high efficiency have become the new characteristics of the refrigeration industry. At the same time, in cold winter and high altitude areas, mechanical equipment needs to operate at lower temperatures, and the low-temperature fluidity and additive compatibility of the oil will decrease, thus affecting the normal progress of industrial production. These changes and developments have promoted the development of refrigeration oil research and production, and at the same time put forward higher requirements for the performance and quality of refrigeration oil.

[0007] Although the production process of traditional refrigeration oil base oil is highly sensitive to additives, it has fatal defects such as severe environmental pollution and poor thermal oxidation stability of the base oil, and is being gradually replaced by new processes.

[0008] The patent with publication number CN 105969422A discloses a method for producing solvent oil by adsorption separation, which uses C9-C12 intermediate distillate oil as raw material, and includes the following steps: (1) pre-adsorbing the raw material to remove trace sulfur-containing and nitrogen-containing impurities to obtain a refined raw material; (2) the refined raw material is subjected to continuous adsorption separation of aromatics in a three-zone simulated moving bed to obtain common solvent oil containing a desorbent and aromatic solvent oil containing a desorbent; (3) the solvent oil containing a desorbent enters a distillation tower to recover the desorbent, respectively, to obtain common solvent oil and aromatic solvent oil; (4) the common solvent oil and aromatic solvent oil enter a product distillation tower again respectively. The method for producing solvent oil by adsorption separation provided by the present invention can remove aromatics under non-hydrogenation conditions and make comprehensive use of aromatics.

[0009] Preparation method for carbon-10 heavy aromatics low-naphthalene high-boiling-point aromatics solvent (application number: WO2020051885), using C10 heavy aromatics as raw materials, obtaining high boiling point products through multi-stage distillation, and then obtaining carbon-10 high boiling point aromatics solvent through crystallization and separation devices.

[0010] The patent with publication number CN117186967A discloses a highly compatible refrigeration oil, which uses a composite ester as the main base oil and is compounded with an additive formula so as to be used together with R32 refrigerant in a refrigeration system. The refrigeration oil can have good low-temperature compatibility with R32 refrigerant, and the mixed fluid formed with the refrigerant can have a good dissolving viscosity.

[0011] Although the main production routes on the market are environmentally friendly and have good thermal oxidation stability, the base oil does not contain aromatics and has poor compatibility with various additives. Especially under low temperature conditions, the compatibility of the base oil with the refrigerant deteriorates. At the same time, additive precipitation is prone to occur, which will cause the additive to fail and thus cause abnormal operation of the equipment. Summary of the invention

[0012] In order to solve the deficiencies of the prior art, the present invention proposes a solubilizer production process for increasing low-temperature compatibility and a refrigeration oil containing the solubilizer. The purpose is to solve the problem of compatibility of refrigeration oil base oil with additives at low temperatures and the existence of refrigeration oil in refrigerants and the mutual solubility of refrigerants at low temperatures.

[0013] The following content only describes the main parts of the process flow of the present invention. The present invention does not limit the links not mentioned in the process flow, but relevant technical personnel should understand that there should be process technology involved.

[0014] The present invention adopts the following technical solution:

[0015] A production process of a solubilizer, wherein the solubilizer can increase the low-temperature compatibility of a refrigeration oil base oil, and uses paraffin-based naphtha in high-pressure hydrogenation technology as a raw material. The production process comprises the following steps:

[0016] (1) First, the crude oil is passed through an ion exchange membrane filter to remove metal salts, colloids and a small amount of solid impurities in the crude oil to obtain decontaminated naphtha;

[0017] (2) The decontaminated naphtha enters a preheater and is heated to 40-55° C. to obtain preheated oil;

[0018] (3) The preheated oil flows into the fractionation tower to complete fraction cutting, mainly cutting out the fraction with a distillation range of 60-170°C to obtain distillate oil;

[0019] (4) After the distillate oil is extracted from the fractionation tower, it enters the polymerization reactor. Under certain conditions, the low-carbon organic molecules in the distillate oil complete the polymerization reaction to obtain polymerized oil, which contains a large number of polyphenyl ring organic molecules;

[0020] (5) After heat exchange, the polymerized oil enters a light hydrogenation reactor, where the polymerized oil is countercurrently contacted with hydrogen and subjected to a light hydrogenation reaction under the action of a catalyst to obtain refined oil;

[0021] (6) The refined oil is further fractionated in a distillation tower, and the fraction with a distillation range of 180-205°C extracted from the distillation tower is the solubilizer product;

[0022] (7) After being condensed by the condenser, the solubilizer product flows into the solubilizer storage tank or is directly pumped into the refrigeration oil production unit for component blending.

[0023] In the step (2), the decontaminated naphtha is preheated by a preheater to reduce the consumption of heat energy in the distillation tower. The heat source in the preheater comes from the condenser in step (7) to condense the solubilizing agent, thereby realizing the internal heat circulation of the solubilizing agent production process.

[0024] In the step (3), a condenser and a reflux tank are provided at the top of the fractionation tower, and a portion of the top product is condensed and sent back to the fractionation tower, and the other portion is sent to the catalytic reforming unit for producing fuel gas or gasoline blending components;

[0025] A reboiler is provided at the bottom of the fractionation tower, and the materials at the bottom of the tower are heated and vaporized and then returned to the bottom of the tower to further provide heat for fractionation;

[0026] The heat of the reboiler comes from the condenser in step (7) condensing the solubilizing agent, thereby realizing the internal circulation of heat in the solubilizing agent production process.

[0027] In the step (3), the operating pressure of the fractionation tower is 0.2-0.35 MPa, the top temperature is 55-75° C., the bottom temperature is 55-180° C., and the reflux ratio is 0.5-0.8.

[0028] In the step (4), the polymerization reaction catalyst flows out of the reactor from top to bottom as the reaction progresses and is lifted to the regenerator. The regenerated catalyst is sent to the polymerization reactor to catalyze the polymerization reaction of the distillate oil, thereby completing one cycle.

[0029] The carrier of the polymerization reaction catalyst is selected from corn stalks, fly ash, pulp sludge, nano titanium oxide, and clay as raw materials to make a porous carrier, and the active component is selected from magnesium, cobalt, nickel, cesium, palladium, beryllium, manganese, zinc, cerium, platinum or rhenium, which is a polyaromatic polymerization directional reaction catalyst.

[0030] In the step (4), the operating pressure of the polymerization reactor is 1.5-2 MPa and the operating temperature is 400-450°C.

[0031] In the step (5), a cyclone separator is arranged on the top of the light hydrogenation reactor to separate hydrogen and the refined oil and hydrogenation catalyst carried away by it. The separated hydrogen returns to the hydrogen storage tank, and the refined oil and catalyst return to the light hydrogenation reactor via the cyclone separator feed leg.

[0032] In the step (5), in the light hydrogenation reactor, some N, S and P elements in the polymerized oil molecules are removed, and unstable double bonds and triple bonds due to incomplete polymerization are hydrogenated and saturated, so that the refined oil obtained is aromatic hydrocarbons and single-bond alkanes, and contains a certain amount of N, S and P elements, so that the final solubilizer product has better stability, antioxidant properties and anti-wear properties.

[0033] In step (5), the operating pressure of the light hydrogenation reactor is 1-1.5 MPa, the reaction temperature is 235-340° C., and the hydrogen-to-oil ratio is 50-100 Nm3 / m3;

[0034] The hydrogenation catalyst adopts an amorphous silicon-aluminum composite carrier, and the active component oxides loaded are nickel oxide, molybdenum oxide, tungsten oxide and phosphorus oxide.

[0035] In the step (6), a condenser and a reflux tank are provided at the top of the distillation tower, and a portion of the top product is condensed and sent back to the distillation tower, and the other portion is sent to the aromatics extraction unit for producing benzene, toluene and xylene products;

[0036] A reboiler is provided at the bottom of the tower. The material at the bottom of the tower is heated and vaporized and then returns to the bottom of the tower to further provide heat for the distillation of the refined oil.

[0037] In the step (6), the operating pressure of the distillation tower is 1.5-3 kPa, the top temperature is 121-133° C., the bottom temperature is 143-151° C., and the reflux ratio is 0.5-1.5.

[0038] The refrigeration oil containing the above solubilizer comprises the following components:

[0039] Base oil: 80-98;

[0040] The base oil is a mineral base oil, mainly cycloalkyl U30℃ and N4006 (without aromatics);

[0041] Antioxidant: 1-2.3;

[0042] The antioxidant is a phenolic compound, preferably 2,6-di-tert-butyl-p-cresol;

[0043] Extreme pressure anti-wear agent: 0.8-2;

[0044] The extreme pressure anti-wear agent is a compound of one or more phosphate compounds, preferably tricresyl phosphate (TCP), tricresyl phosphate (T306) and tricresyl thiophosphate (T309);

[0045] Solubilizer: 5-18;

[0046] The solubilizer is a high boiling point compound, the main component of which is polyphenyl aromatic hydrocarbons.

[0047] Furthermore: the refrigeration oil containing the solubilizer has good compatibility with the refrigerant;

[0048] The refrigerant is an environmentally friendly low-carbon saturated hydrocarbon, preferably propane (R290), butane (R600) and isobutane (R600a).

[0049] The beneficial technical effects achieved by adopting the above technical solution are:

[0050] 1. The raw oil is passed through an ion exchange membrane filter to remove metal salts, colloids and a small amount of solid impurities doped in the raw oil to obtain decontaminated naphtha; the decontaminated naphtha enters a preheater to heat the decontaminated naphtha to 40-55°C to obtain preheated oil; the preheated oil flows into a fractionation tower to complete fraction cutting, mainly cutting out fractions with a distillation range of 60-170°C to obtain distillate oil; the distillate oil is extracted from the fractionation tower and enters a polymerization reactor, and low-carbon organic molecules in the distillate oil complete polymerization reaction under certain conditions to obtain polymerized oil; the polymerized oil enters a light hydrogenation reactor after heat exchange, and the polymerized oil is countercurrently contacted with hydrogen in the reactor, and a light hydrogenation reaction is performed under the action of a catalyst to obtain refined oil; the refined oil is further fractionated in the distillation tower, and the fraction with a distillation range of 180-205°C extracted from the distillation tower is the solubilizer product; the solubilizer product is condensed in a condenser and flows into a solubilizer storage tank or is directly pumped into a refrigeration oil production unit for component blending. The production process route of low-temperature solubilizer for refrigeration oil has been broadened and production efficiency has been improved.

[0051] 2. It is environmentally friendly, reduces environmental pollution and energy consumption in the production process, and simplifies the production process.

[0052] 3. Improved the solubility of refrigeration oil at low temperatures and its miscibility with refrigerants.

[0053] 4. It weakens the precipitation of additives at low temperatures and strengthens the effect of additives, thereby improving the performance and quality of refrigeration oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0054] Figure 1 It is a schematic diagram of the production process system of the solubilizer;

[0055] Figure 2 The flowchart of the production process of the solubilizer is shown below;

[0056] Figure 3 The figure is a comparison chart of the experimental results of refrigeration oil containing the solubilizer.

[0057] In the figure:

[0058] 1. ion exchange membrane filter, 2. preheater, 3. fractionation tower, 31. first condenser, 32. first reflux tank, 33. first reboiler, 4. polymerization reactor, 41. regenerator, 42. heat exchanger, 5. light hydrogenation reactor, 51. cyclone separator, 52. hydrogen storage tank, 6. distillation tower, 61. second condenser, 62. second reflux tank, 63. second reboiler, 7. third condenser, 8. storage tank. DETAILED DESCRIPTION

[0059] Combined with Figures 1 to 3The technical solutions in the embodiments of the present invention are described clearly and completely. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0060] Embodiment 1:

[0061] The present invention uses a unique preparation process and formula design to enable the refrigeration oil to maintain good fluidity and stability at low temperatures, maintain excellent miscibility with the refrigerant at low temperatures, and at the same time enable the refrigeration oil to meet the social requirements of green environmental protection. This innovative solution will bring important technological progress and economic benefits to the refrigeration equipment industry.

[0062] The following content only describes the main parts of the process flow of the present invention. The present invention does not limit the links not mentioned in the process flow, but relevant technical personnel should understand that there should be process technology involved.

[0063] The production process of the solubilizer is:

[0064] The paraffin-based naphtha in high-pressure hydrogenation technology is used as the raw material. The raw oil is first passed through an ion exchange membrane filter to remove metal salts, colloids and a small amount of solid impurities in the raw oil to obtain decontaminated naphtha, avoiding catalyst poisoning in subsequent processes and reducing the risks of coking and blockage of pipelines and equipment.

[0065] A preheater is connected after the filter to heat the decontaminated naphtha to 40-55°C, and the preheated oil flows into the fractionation tower for fractionation. Setting up a preheater can achieve energy saving and consumption reduction in the overall production process. This is reflected in two aspects: first, the preheater heats the decontaminated naphtha to a certain temperature, which can reduce the consumption of heat energy in the fractionation tower; second, the heat source energy in the preheater comes from the solubilizer obtained from the final distillation, thereby realizing the internal circulation of heat in the production process.

[0066] The preheated oil is fractionated in the distillation tower, mainly cutting out the fraction between 60-170℃ to obtain distillate oil. The temperature of the preheated oil is close to the lower limit of the distillation range, so it is easier to obtain the required distillate oil. A condenser and a reflux tank are set at the top of the distillation tower. After the top product is condensed, part of it is sent back to the distillation tower, and the other part is sent to the catalytic reforming unit for the production of gas or gasoline blending components. A reboiler is set at the bottom of the tower. The bottom material is heated and vaporized and then returned to the bottom of the tower to provide further heat for fractionation. The heat of the reboiler of the distillation tower also comes from the solubilizer obtained by the final distillation, so that the solubilizer product is fully utilized.

[0067] The operating pressure of the distillation tower is 0.2-0.35MPa, the top temperature is 55-75°C, the bottom temperature is 55-180°C, and the reflux ratio is 0.5-0.8.

[0068] The distillate oil is drawn out of the fractionation tower and enters the polymerization reactor. The polymerization reactor is a moving bed reactor that can operate continuously. In the polymerization reactor, the low-carbon organic molecules in the distillate oil complete the polymerization reaction under certain conditions to obtain polymerized oil, which contains a large number of polyphenyl ring organic molecules. The polymerization catalyst flows out of the reactor from top to bottom as the reaction progresses and is lifted to the regenerator. The regenerated catalyst is sent to the polymerization reactor to catalyze the polymerization reaction of the distillate oil, thus completing a cycle.

[0069] The carrier of the polymerization reaction catalyst is selected from a porous carrier made from corn stalks, fly ash, pulp sludge, nano-titanium oxide, clay, etc. as raw materials, and the active component is selected from magnesium, cobalt, nickel, cesium, palladium, beryllium, manganese, zinc, cerium, platinum or rhenium, etc., preferably a polyaromatic polymerization directional reaction catalyst.

[0070] The operating pressure of the polymerization reactor is 1.5-2MPa and the operating temperature is 400-450°C.

[0071] The polymerized oil enters the light hydrogenation reactor after heat exchange. In the reactor, the polymerized oil contacts with hydrogen in countercurrent, and a light hydrogenation reaction is carried out under the action of a catalyst to obtain refined oil. A cyclone separator is arranged on the top of the light hydrogenation reactor to separate hydrogen and the refined oil and hydrogenation catalyst carried out by it. The separated hydrogen returns to the hydrogen storage tank, and the refined oil and catalyst return to the light hydrogenation reactor through the cyclone separator legs. In the light hydrogenation reactor, some elements such as N, S and P in the polymerized oil molecules are removed, and the unstable double bonds and triple bonds due to incomplete polymerization are hydrogenated and saturated. The refined oil obtained in this way is basically aromatic hydrocarbons and single-bond alkanes, and contains a certain amount of elements such as N, S and P, which can make the final solubilizer product have better stability, antioxidant properties and anti-wear properties.

[0072] The light hydrogenation reactor has an operating pressure of 1-1.5 MPa, a reaction temperature of 235-340°C, and a hydrogen-to-oil ratio of 50-100 Nm3 / m3. The hydrogenation catalyst uses an amorphous silicon-aluminum composite carrier, and the active component oxides loaded are nickel oxide, molybdenum oxide, tungsten oxide, phosphorus oxide, etc.

[0073] The refined oil is further fractionated in the distillation tower. The distillation tower adopts a vacuum distillation method. A condenser and a reflux tank are set at the top of the distillation tower. After the top product is condensed, part of it is sent back to the distillation tower, and the other part is sent to the aromatic extraction unit for the production of benzene, toluene, xylene and other products. A reboiler is set at the bottom of the tower. The bottom material is heated and vaporized and then returned to the bottom of the tower to further provide heat for the distillation of the refined oil. The fraction with a distillation range of 180-205°C extracted from the distillation tower is the solubilizer product of the present invention.

[0074] The operating pressure of the distillation tower is 1.5-3kPa, the top temperature is 121-133°C, the bottom temperature is 143-151°C, and the reflux ratio is 0.5-1.5.

[0075] The solubilizer product obtained from the final distillation is condensed and flows into the storage tank. It can also be directly pumped into the refrigeration oil production unit for component blending.

[0076] Embodiment 2:

[0077] The solubilizer production equipment comprises an ion exchange membrane filter 1, a preheater 2, a fractionation tower 3, a polymerization reactor 4, a light hydrogenation reactor 5, and a rectification tower 6 which are connected in sequence.

[0078] The provision of a preheater 2 can achieve energy conservation and consumption reduction in the overall production process. This is reflected in two aspects: first, the preheater heats the decontaminated naphtha to a certain temperature, which can reduce the consumption of heat energy in the fractionation tower; second, the heat source energy in the preheater comes from the solubilizer obtained from the final distillation, thereby achieving internal heat circulation in the production process.

[0079] The outlet at the upper end of the preheater is connected to the third condenser. The preheater is heated to 40-55° C. and a small amount of distillate is produced, which can be directly used as a solubilizing agent.

[0080] A first condenser 31 and a first reflux tank 32 are provided at the top of the distillation tower 3. The first reflux tank is connected to the distillation tower, and the first reflux tank is also connected to the catalytic reforming unit. After the top product is condensed, part of it is sent back to the distillation tower, and the other part is sent to the catalytic reforming unit for producing fuel gas or gasoline blending components.

[0081] The first reboiler 33 is provided at the bottom of the fractionation tower, and the first reboiler is connected to the bottom of the fractionation tower. The materials at the bottom of the tower are heated and vaporized and then returned to the bottom of the tower. Heat is further provided for fractionation. The heat of the reboiler of the fractionation tower also comes from the solubilizer obtained by the final distillation, so that the solubilizer product is fully utilized.

[0082] In the polymerization reactor, the low carbon number organic molecules in the distillate oil complete polymerization under certain conditions to obtain polymerized oil, which contains a large number of polyphenyl ring organic molecules. The polymerization catalyst flows out of the reactor from top to bottom as the reaction progresses and is lifted to the regenerator 41. The regenerated catalyst is sent to the polymerization reactor to catalyze the polymerization reaction of the distillate oil, thereby completing one cycle.

[0083] The polymerization reactor 5 is connected to the light hydrogenation reactor 5 via a heat exchanger 42 .

[0084] The polymerized oil enters the light hydrogenation reactor 5 after heat exchange. In the reactor, the polymerized oil contacts with hydrogen in countercurrent and performs a light hydrogenation reaction under the action of the catalyst to obtain refined oil. A cyclone separator 51 is arranged on the top of the light hydrogenation reactor to separate hydrogen and the refined oil and hydrogenation catalyst carried out by it. The separated hydrogen returns to the hydrogen storage tank 52, and the refined oil and catalyst return to the light hydrogenation reactor through the cyclone separator feed leg.

[0085] The top of the distillation tower 6 is provided with a second condenser 61 and a second reflux tank 62, the second reflux tank 62 is connected to the distillation tower, and the second reflux tank is also connected to the aromatic extraction unit. After condensation, part of the top product of the distillation tower is sent back to the distillation tower, and the other part is sent to the aromatic extraction unit for the production of benzene, toluene and xylene products. A second reboiler is provided at the bottom of the tower, and the bottom material is heated and vaporized and then returned to the bottom of the tower to further provide heat for the distillation of the refined oil.

[0086] The distillation tower 6 is connected to a storage tank 8 via a third condenser 7. Alternatively, the distillation tower is connected to a refrigeration oil production unit via a third condenser.

[0087] The heat exchanger and the third condenser are connected to the preheater and the first reboiler through the heat source transmission pipeline. The heat source energy in the preheater comes from the solubilizer obtained by the final distillation, thereby realizing the internal heat circulation of the production process. The heat of the fractionation tower reboiler also comes from the solubilizer obtained by the final distillation, so that the heat of the solubilizer product is fully utilized.

[0088] Embodiment 3:

[0089] The present invention also provides a method for using the solubilizer in refrigeration oil. The figures on the formula composition are all mass percentages except for the units indicated.

[0090] The formula of the refrigeration oil containing the above solubilizer is as follows:

[0091] Base oil: 80-98.

[0092] The base oil is a mineral base oil, mainly cycloalkyl U30°C and N4006 (containing no aromatics).

[0093] Antioxidant: 1-2.3

[0094] The antioxidant is a phenolic compound, preferably 2,6-di-tert-butyl-p-cresol.

[0095] Extreme pressure anti-wear agent: 0.8-2

[0096] The extreme pressure anti-wear agent is a compound of one or more phosphate compounds, preferably tricresyl phosphate (TCP), tricresyl phosphate (T306) and tricresyl thiophosphate (T309). If necessary, the specific ratio can be flexibly adjusted according to the application scenario and environmental protection requirements.

[0097] Solubilizer: 5-18.

[0098] The solubilizer is a high boiling point compound obtained by the aforementioned production process, and its main component is polyphenyl aromatic hydrocarbons.

[0099] The refrigerator oil containing the solubilizer is well compatible with the refrigerant. The refrigerant is an environmentally friendly low-carbon saturated hydrocarbon, preferably propane (R290), butane (R600) and isobutane (R600a).

[0100] Embodiment 4:

[0101] The base oil is commercially available aromatic-free U30-℃ with a content of 88.

[0102] The amount of antioxidant added is 0.

[0103] The extreme pressure anti-wear agent is tritolyl phosphate (TCP) with a content of 2.

[0104] The solubilizer is the solubilizer product, and its content is 10.

[0105] Embodiment 5:

[0106] The base oil is a commercially available aromatic-free U30-℃ with a content of 83.

[0107] The amount of antioxidant added is 0.

[0108] The extreme pressure anti-wear agent is tritolyl phosphate (TCP) with a content of 2.

[0109] The solubilizer is the solubilizer product, and its content is 15.

[0110] Comparative Example 1:

[0111] The base oil is commercially available aromatic-free U30-℃ with a content of 98.

[0112] The amount of antioxidant added is 0.

[0113] The extreme pressure anti-wear agent is tritolyl phosphate (TCP) with a content of 2.

[0114] The amount of solubilizer added was 0.

[0115] According to GB / T 12577-1990 Determination of Flocculation Point of Refrigeration Oil, the blended refrigeration oils in Example 4, Example 5 and Comparative Example 1 were tested.

[0116] The test uses clean dry ice as a cold bath, selects isobutane (R600a) as a refrigerant, and the cooling rate of the test tube is 1°C / min. Each embodiment and comparative example is tested 6 times, and the arithmetic mean is taken as the measurement result. The test results are listed in Table 1.

[0117] Table 1 Comparison table of Example 4, Example 5 and Comparative Example 1:

[0118] Comparison Items Example 1 Example 2 Comparative Example 1 No aromatics U30-℃ content 88 83 98 Antioxidant addition amount 0 0 0 Extreme pressure anti-wear agent tritolyl phosphate (TCP) content 2 2 2 Solubilizer content 10 15 0 Flocculation point (℃) -53 -49 -23

[0119] It can be seen from Table 1 that, when other variables are the same, adding a solubilizer can reduce the flocculation point temperature of the refrigeration oil.

[0120] Figure 3 From left to right in the figure are three groups of test samples of Example 4, Example 5 and Comparative Example 1 with 10%, 15% and 0% solubilizer addition. It can be seen from the figure that the refrigerator oil without adding solubilizer at low temperature is flocculated and milky white. When the solubilizer addition is 10%, the appearance of the refrigerator oil at low temperature is clear and transparent, which greatly improves the compatibility of the oil with additives at low temperature.

[0121] Experiments have shown that adding 5% of solubilizer to refrigeration oil can improve the compatibility of oil with additives at low temperatures. As the amount of solubilizer added to refrigeration oil increases, the compatibility of oil with additives at low temperatures improves, and the flocculation point temperature value of refrigeration oil decreases. However, when the amount of solubilizer added to refrigeration oil is greater than 18%, there is little change. In actual production, according to the application environment requirements of refrigeration oil, the amount of solubilizer added to refrigeration oil is determined so that the refrigeration oil can still maintain good fluidity and stability at low temperatures, and maintain excellent miscibility with the refrigerant at low temperatures.

[0122] It should be noted that, in this article, positional terms such as top, bottom, left, right, etc. are used only for convenience of description. Moreover, the terms "include", "comprises", or any other variations thereof are intended to cover non-exclusive inclusion, so that a process, method, article, or device including a series of elements includes not only those elements, but also other elements not explicitly listed, or also includes elements inherent to such process, method, article, or device.

[0123] Of course, the above description is only a preferred embodiment of the present invention, and the present invention is not limited to the above-mentioned embodiments. It should be noted that all equivalent substitutions and obvious deformation forms made by any technician familiar with the field under the guidance of this specification fall within the essential scope of this specification and should be protected by the present invention.

Claims

1. A production process of a solubilizing agent, characterized in that: The solubilizer can increase the low-temperature compatibility of the refrigeration oil base oil, and uses paraffin-based naphtha in high-pressure hydrogenation technology as a raw material. The production process includes the following steps: (1) First, the crude oil is passed through an ion exchange membrane filter to remove metal salts, colloids and a small amount of solid impurities in the crude oil to obtain decontaminated naphtha; (2) The decontaminated naphtha enters a preheater and is heated to 40-55° C. to obtain preheated oil; (3) The preheated oil flows into the fractionation tower to complete fraction cutting, mainly cutting out the fraction with a distillation range of 60-170°C to obtain distillate oil; (4) After the distillate oil is extracted from the fractionation tower, it enters the polymerization reactor. Under certain conditions, the low-carbon organic molecules in the distillate oil complete the polymerization reaction to obtain polymerized oil, which contains a large number of polyphenyl ring organic molecules; (5) After heat exchange, the polymerized oil enters a light hydrogenation reactor, where the polymerized oil is countercurrently contacted with hydrogen and subjected to a light hydrogenation reaction under the action of a catalyst to obtain refined oil; (6) The refined oil is further fractionated in a distillation tower, and the fraction with a distillation range of 180-205°C extracted from the distillation tower is the solubilizer product; (7) After being condensed by the condenser, the solubilizer product flows into the solubilizer storage tank or is directly pumped into the refrigeration oil production unit for component blending.

2. A production process of a solubilizing agent according to claim 1, characterized in that: In the step (2), the decontaminated naphtha is preheated by a preheater to reduce the consumption of heat energy in the distillation tower. The heat source in the preheater comes from the condenser in step (7) to condense the solubilizing agent, thereby realizing the internal heat circulation of the solubilizing agent production process.

3. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (3), a condenser and a reflux tank are provided at the top of the fractionation tower, and a portion of the top product is condensed and sent back to the fractionation tower, and the other portion is sent to the catalytic reforming unit for producing fuel gas or gasoline blending components; A reboiler is provided at the bottom of the fractionation tower, and the materials at the bottom of the tower are heated and vaporized and then returned to the bottom of the tower to further provide heat for fractionation; The heat of the reboiler comes from the condenser in step (7) condensing the solubilizing agent, thereby realizing the internal circulation of heat in the solubilizing agent production process.

4. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (3), the operating pressure of the fractionation tower is 0.2-0.35 MPa, the top temperature is 55-75° C., the bottom temperature is 55-180° C., and the reflux ratio is 0.5-0.

8.

5. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (4), the polymerization reaction catalyst flows out of the reactor from top to bottom as the reaction progresses and is lifted to the regenerator. The regenerated catalyst is sent to the polymerization reactor to catalyze the polymerization reaction of the distillate oil, thereby completing one cycle.

6. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (4), the operating pressure of the polymerization reactor is 1.5-2 MPa and the operating temperature is 400-450°C.

7. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (5), a cyclone separator is arranged on the top of the light hydrogenation reactor to separate hydrogen and the refined oil and hydrogenation catalyst carried away by it. The separated hydrogen returns to the hydrogen storage tank, and the refined oil and catalyst return to the light hydrogenation reactor via the cyclone separator feed leg.

8. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (5), in the light hydrogenation reactor, some N, S and P elements in the polymerized oil molecules are removed, and unstable double bonds and triple bonds due to incomplete polymerization are hydrogenated and saturated, so that the refined oil obtained is aromatic hydrocarbons and single-bond alkanes, and contains a certain amount of N, S and P elements, so that the final solubilizer product has better stability, antioxidant properties and anti-wear properties.

9. The production process of a solubilizing agent according to claim 1, characterized in that: In step (5), the operating pressure of the light hydrogenation reactor is 1-1.5 MPa, the reaction temperature is 235-340° C., and the hydrogen-to-oil ratio is 50-100 Nm3 / m3; The hydrogenation catalyst adopts an amorphous silicon-aluminum composite carrier, and the active component oxides loaded are nickel oxide, molybdenum oxide, tungsten oxide and phosphorus oxide.

10. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (6), a condenser and a reflux tank are provided at the top of the distillation tower, and a portion of the top product is condensed and sent back to the distillation tower, and the other portion is sent to the aromatics extraction unit for producing benzene, toluene and xylene products; A reboiler is provided at the bottom of the tower. The material at the bottom of the tower is heated and vaporized and then returns to the bottom of the tower to further provide heat for the distillation of the refined oil.

11. The production process of a solubilizing agent according to claim 1, characterized in that: In the step (6), the operating pressure of the distillation tower is 1.5-3 kPa, the top temperature is 121-133° C., the bottom temperature is 143-151° C., and the reflux ratio is 0.5-1.

5.

12. A refrigerating machine oil containing the solubilizing agent according to any one of claims 1 to 11, characterized in that: The formula of the refrigeration oil comprises the following components: Base oil: 80-98; The base oil is a mineral base oil, mainly cycloalkyl U30℃ and N4006 (without aromatics); Antioxidant: 1-2.3; The antioxidant is a phenolic compound, preferably 2,6-di-tert-butyl-p-cresol; Extreme pressure anti-wear agent: 0.8-2; The extreme pressure anti-wear agent is a compound of one or more phosphate compounds, preferably tricresyl phosphate (TCP), tricresyl phosphate (T306) and tricresyl thiophosphate (T309); Solubilizer: 5-18; The solubilizer is a high boiling point compound, the main component of which is polyphenyl aromatic hydrocarbons.

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