Hydrogen peroxide concentration system

Abstract

The utility model provides a hydrogen peroxide concentration system which comprises a rectification device, a first heat exchanger and a heat supply heat pump device, and the first heat exchanger is used for concentrating hydrogen peroxide; the first heat exchanger comprises a first channel and a second channel, the heat supply heat pump device comprises a first heat exchange loop, a first heat exchange medium circulates in the first heat exchange loop, a heat taking working medium storage component, a compressor and a second heat exchanger are arranged on the first heat exchange loop, and the second heat exchanger is arranged between the heat taking working medium storage component and the compressor. The rectification device is connected with the second heat exchanger, the first heat exchange medium is arranged to provide heat for the first heat exchanger, and the second heat exchanger is arranged to enable steam discharged by the rectification device to exchange heat with the first heat exchange medium. According to the system, steam condensate is gasified again through cyclic compression and utilization of a heating working medium, a heat source is provided for hydrogen peroxide concentration, and the production cost of the hydrogen peroxide concentration process is saved.

Description

Technical Field

[0001] The utility model belongs to the technical field of hydrogen peroxide production, in particular to a hydrogen peroxide concentration system. Background Art

[0002] Propylene oxide (PO) is a downstream derivative of propylene with a production capacity second only to that of polypropylene. It is widely used in the production of many high-value-added chemicals such as propylene glycol, propylene carbonate, polyurethane, and unsaturated resins, and plays an irreplaceable role in the fields of transportation electronics, construction furniture, daily chemicals, and medicine. In recent years, with the continuous improvement of human production and living standards, the consumption of PO has shown an increasing trend year by year. The preparation methods of PO include the co-oxidation route with organic peroxide as the oxidant and the hydrogen peroxide method for preparing propylene oxide (HPPO). The HPPO process has the advantages of high atomic utilization, clean and efficient, and simple process, and occupies an important position in the production of propylene oxide.

[0003] Propylene oxide can be efficiently obtained by synthesizing propylene oxide from hydrogen peroxide and propylene in one step (HPPO method). Hydrogen peroxide is a clean oxidant that can be used as an oxidant, bleaching agent, disinfectant, and can also be used in the production of inorganic and organic peroxides, and can also be used in medical chemical analysis processes. With the increasing demand for PO, the demand for high-concentration hydrogen peroxide has also continued to increase; in existing hydrogen peroxide devices, hydrogen peroxide concentration mainly uses fresh steam as the heat source for the distillation tower and falling film evaporator, which has the disadvantages of huge energy consumption, low thermal efficiency, and high production cost. Utility Model Content

[0004] In view of this, the utility model aims to propose a hydrogen peroxide concentration system, which re-gasifies the steam condensate through the circulation and compression of the heat extracting medium to provide a heat source for hydrogen peroxide concentration. The utility model aims to use electric energy instead of fresh steam, greatly reduce energy consumption, and save production costs in the hydrogen peroxide concentration process.

[0005] In order to achieve the above object, the technical solution of the utility model is implemented as follows:

[0006] A hydrogen peroxide concentration system comprises a distillation device, a first heat exchanger and a heat supply heat pump device, wherein the first heat exchanger is used for concentrating hydrogen peroxide;

[0007] The first heat exchanger comprises a first channel and a second channel, hydrogen peroxide flows in the first channel, and a heat exchange medium capable of exchanging heat with hydrogen peroxide flows in the second channel;

[0008] The heat supply heat pump device comprises a first heat exchange circuit, a first heat exchange medium flows in the first heat exchange circuit, a heat extraction medium storage component, a compressor and a second heat exchanger are arranged on the first heat exchange circuit, the heat extraction medium storage component can store the first heat exchange medium, the second heat exchanger is arranged between the heat extraction medium storage component and the compressor, and the distillation device is connected to the second heat exchanger.

[0009] The first heat exchange medium is configured to provide heat to the first heat exchanger, so that the water in the hydrogen peroxide in the first channel is converted into steam and passed into the distillation device to achieve concentration of the hydrogen peroxide.

[0010] The second heat exchanger is configured to enable the steam discharged from the distillation device to exchange heat with the first heat exchange medium, so that the first heat exchange medium evaporates back into the compressor.

[0011] Furthermore, the first heat exchange circuit is connected to the second channel, one end of the second channel is connected to the exhaust port of the compressor, and the other end of the second channel is connected to the heat extraction medium storage component.

[0012] Furthermore, a third heat exchanger is also provided on the first heat exchange circuit, and the third heat exchanger is provided between the exhaust port of the compressor and the heat extracting medium storage component;

[0013] The heat supply heat pump device further comprises a second heat exchange circuit, a second heat exchange medium flows in the second heat exchange circuit, and the third heat exchanger and the steam condensate tank are arranged on the second heat exchange circuit;

[0014] The second channel is connected to the second heat exchange circuit, one end of the second channel is connected to the third heat exchanger, and the other end of the second channel is connected to the steam condensate tank;

[0015] The third heat exchanger is configured to enable the first heat exchange medium to exchange heat with the second heat exchange medium to provide heat for the first heat exchanger.

[0016] Furthermore, the second heat exchanger is connected to the steam condensate tank, and the liquid after the steam discharged from the distillation device is heat-exchanged by the second heat exchanger enters the steam condensate tank.

[0017] Furthermore, it also includes a vacuum pump, and the non-condensable gas of the distillation device after heat exchange in the second heat exchanger and the non-condensable gas of the first heat exchanger are extracted through the vacuum pump.

[0018] Furthermore, it also includes a vacuum pump, and the non-condensable gas of the distillation device after heat exchange in the second heat exchanger is extracted through the vacuum pump.

[0019] Further, it also includes a liquid level control branch connected to the first channel, the liquid level control branch is provided with a liquid level control valve, and the liquid level control valve is configured to control the amount of hydrogen peroxide in the first channel by adjusting the feed amount of dilute hydrogen peroxide; and / or it also includes a temperature control branch connected to the first channel, the temperature control branch is provided with a temperature control valve, and the temperature control valve is configured to control the temperature of hydrogen peroxide in the first channel by adjusting the discharge amount of concentrated hydrogen peroxide.

[0020] Furthermore, it also includes a pressure regulating branch, the two ends of which are connected to the two sides of the vacuum pump, and the pressure regulating branch is configured to control the pressure and temperature of the top part of the distillation device by controlling the vacuum pump; and / or the pressure range of the top part of the distillation device is 6 to 10 kPaA, and the temperature is 36 to 46°C.

[0021] Furthermore, the temperature of the hydrogen peroxide in the first channel is 55-65° C., and the pressure is 8-12 kPaA; and / or the temperature of the steam generated in the second channel is 65-75° C., and the pressure is 25-35 kPaA.

[0022] Furthermore, the condensation temperature of the first heat exchange medium is 75-85°C, and the evaporation temperature is 25-35°C; preferably, the first heat exchange medium includes one or more of n-butane, isobutane, R134a, R245fa, ammonia, and propylene.

[0023] Compared with the prior art, the hydrogen peroxide concentration system described in the utility model has the following advantages:

[0024] The hydrogen peroxide concentration system of the utility model re-gasifies the steam condensate by circulating and compressing the heat medium to provide a heat source for hydrogen peroxide concentration. The utility model aims to use electric energy instead of fresh steam, greatly reduce energy consumption, and save production costs in the hydrogen peroxide concentration process. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] The accompanying drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation on the present invention. In the accompanying drawings:

[0026] Figure 1 This is a schematic diagram of the hydrogen peroxide concentration system described in Example 1 of the utility model;

[0027] Figure 2 This is a schematic diagram of the hydrogen peroxide concentration system described in Example 2 of the present utility model;

[0028] Figure 3This is a schematic diagram of the hydrogen peroxide concentration system described in Comparative Example 1 of the present invention.

[0029] Description of reference numerals:

[0030] 1. Distillation tower; 2. Falling film evaporator; 3. Hydrogen peroxide circulation pump; 4. Steam condensate tank; 5. Condenser; 6. Steam condensate feed pump; 7. Heat medium storage tank; 8. Evaporator; 9. Vacuum pump; 10. Compressor; 11. Gas-liquid separation component; 12. Steam ejector; 13. Top condenser. DETAILED DESCRIPTION

[0031] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.

[0032] In the description of the present utility model, it should be understood that the terms "upper", "lower", "front", "back", "top", "bottom", "inside", etc. indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present utility model, unless otherwise specified, "multiple" means two or more.

[0033] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "connected" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0034] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0035] In the following embodiments, the distillation device is such as a distillation tower 1, the first heat exchanger is such as a falling film evaporator 2, the heat medium storage component is such as a heat medium storage tank 7, the second heat exchanger is such as an evaporator 8, and the third heat exchanger is such as a condenser 5. On the premise of achieving the purpose of the utility model of the present application, it is not limited to this.

[0036] Example 1

[0037] like Figure 1 As shown, a hydrogen peroxide concentration system includes a distillation tower 1, a falling film evaporator 2, a heat supply heat pump device, and a vacuum pump 9.

[0038] The falling film evaporator 2 is used for concentrating hydrogen peroxide, and comprises a first channel and a second channel. Hydrogen peroxide flows in the first channel, and a heat exchange medium capable of exchanging heat with hydrogen peroxide flows in the second channel.

[0039] The heat supply heat pump device comprises a first heat exchange circuit, in which a first heat exchange medium flows, and the first heat exchange circuit is provided with a heat extraction medium storage tank 7, a compressor 10 and an evaporator 8, the heat extraction medium storage tank 7 can store the first heat exchange medium, the evaporator 8 is arranged between the heat extraction medium storage tank 7 and the compressor 10, and the distillation tower 1 is connected to the evaporator 8; Figure 1 As shown, the first heat exchange loop is also connected to the second channel, one end of the second channel is connected to the exhaust port of the compressor 10, and the other end of the second channel is connected to the heat medium storage tank 7. Those skilled in the art will appreciate that the specific structure of the heat medium storage tank 7 is not restrictive, as long as the heat medium can be stored so that the heat medium circulates in the first heat exchange loop to ensure the supply of the heat medium.

[0040] The first heat exchange medium is configured to provide heat for the falling film evaporator 2, so that the water in the hydrogen peroxide in the first channel is converted into steam and passed into the distillation tower 1 to achieve the concentration of the hydrogen peroxide; the evaporator 8 is configured to enable the steam discharged from the distillation tower 1 to exchange heat with the first heat exchange medium, so that the first heat exchange medium evaporates back into the compressor 10.

[0041] The non-condensable gas of the distillation tower 1 after heat exchange in the evaporator 8 is extracted through the vacuum pump 9; the two sides of the vacuum pump 9 are also connected to the two ends of the pressure regulating branch, and the pressure regulating branch is configured to control the pressure and temperature of the top part of the distillation tower 1 by controlling the vacuum pump 9; and / or the pressure range of the top part of the distillation tower 1 is 6 to 10 kPaA, and the temperature is 36 to 46°C.

[0042] The first channel is also provided with a liquid level control branch connected thereto, and a liquid level control valve is provided on the liquid level control branch, and the liquid level control valve is configured to control the amount of hydrogen peroxide in the first channel by adjusting the feed amount of dilute hydrogen peroxide; the first channel is also provided with a temperature control branch connected thereto, and a temperature control valve is provided on the temperature control branch, and the temperature control valve is configured to control the temperature of hydrogen peroxide in the first channel by adjusting the discharge amount of concentrated hydrogen peroxide.

[0043] The temperature of the hydrogen peroxide in the first channel is 55-65° C., and the pressure is 8-12 kPaA.

[0044] The condensation temperature of the first heat exchange medium is 75-85°C, and the evaporation temperature is 25-35°C; preferably, the first heat exchange medium can be one or more of n-butane, isobutane, R134a, R245fa, ammonia, and propylene. It should be noted that the present application does not impose any restrictions on the specific type of the first heat exchange medium, as long as the condensation temperature of the first heat exchange medium is 75-85°C, and the evaporation temperature is 25-35°C, that is, it can meet the heat supply demand of the hydrogen peroxide in the first channel of the falling film heat exchanger 2, and those skilled in the art can set it according to actual conditions.

[0045] The outlet of the compressor 10 is provided with a flow meter, which can detect the condensation amount of the heat extracting medium in the condenser 5. The compressor 10 is driven by a motor; the inlet of the compressor 10 is provided with a pressure control valve, and the compressor 10 is provided with a return valve. The temperature, pressure and flow of the heat extracting medium at the outlet of the compressor 10 are adjusted by adjusting the pressure control valve and the return valve at the inlet of the compressor 10. It should be noted that the compressor 10 can be a variable frequency compressor or a fixed frequency compressor; the number of compressors 10 can be one or more; multiple compressors 10 can be used in series or in parallel; that is, the adjustment of the frequency of the compressor and the heat supply of the first heat exchange circuit by changing the type, number or connection method of the compressor 10 does not deviate from the basic principles of this application and falls within the protection scope of this application.

[0046] The compressor 10 is also connected to a gas-liquid separation component 11 . The specific structure of the gas-liquid separation component 11 is not restrictive, as long as it can prevent the liquid heat exchange medium from entering the compressor 10 .

[0047] Working principle:

[0048] The heat extracting medium evaporates in the evaporator 8, enters the gas-liquid separation component 11 for liquid separation, and then enters the compressor 10 for compression. The heat extracting medium at the outlet of the compressor 10 directly enters the second channel of the falling film evaporator 2 to exchange heat with the hydrogen peroxide in the first channel. The first channel of the falling film evaporator 2 generates steam and enters the distillation tower 1. The heat extracting medium after heat exchange enters the heat extracting medium storage tank 7 and then enters the evaporator 8. The falling film evaporator 2 is provided with a hydrogen peroxide circulation pump 3, and a rare hydrogen peroxide feed and a concentrated hydrogen peroxide discharge are arranged on the circulation pipeline. There is pure water feed at the top of the distillation tower 1, concentrated hydrogen peroxide is produced at the bottom of the tower, and water vapor produced at the top of the tower enters the evaporator 8. The condensed liquid enters the steam condensate tank 4, and the non-condensable gas is discharged through the vacuum pump 9.

[0049] The implementation results show that the power consumption for producing one ton of concentrated hydrogen peroxide is 240 to 260 kW. Based on an electricity price of 0.5 yuan per kilowatt-hour, the energy consumption cost for producing one ton of concentrated hydrogen peroxide is 120 to 130 yuan. Compared with the existing hydrogen peroxide concentration devices on the market that use fresh steam as a heat source, the energy consumption cost for producing one ton of concentrated hydrogen peroxide is reduced by about 32% to 34%.

[0050] Example 2

[0051] like Figure 2 As shown, a hydrogen peroxide concentration system includes a distillation tower 1, a falling film evaporator 2, a heat supply heat pump device, a condenser 5, and a vacuum pump 9.

[0052] The falling film evaporator 2 is used for concentrating hydrogen peroxide, and comprises a first channel and a second channel. Hydrogen peroxide flows in the first channel, and a heat exchange medium capable of exchanging heat with hydrogen peroxide flows in the second channel.

[0053] The heat supply heat pump device includes a first heat exchange circuit, in which a first heat exchange medium flows, and a heat extraction medium storage tank 7, a compressor 10 and an evaporator 8 are provided on the first heat exchange circuit. The heat extraction medium storage tank 7 can store the first heat exchange medium, and the evaporator 8 is arranged between the heat extraction medium storage tank 7 and the compressor 10, and the distillation tower 1 is connected to the evaporator 8; the pressure drop of water vapor in the evaporator 8 needs to be less than 3kPa, and the heat exchanger type of the evaporator 8 can be BXM, BKU, BKM, falling film evaporator, etc.

[0054] The first heat exchange circuit is also provided with a condenser 5, which is provided between the exhaust port of the compressor 10 and the heat medium storage tank 7; the heat supply heat pump device also includes a second heat exchange circuit, in which a second heat exchange medium flows, and the second heat exchange circuit is provided with a condenser 5 and a steam condensate tank 4; the second channel is connected to the second heat exchange circuit, one end of the second channel is connected to the condenser 5, and the other end of the second channel is connected to the steam condensate tank 4; the condenser 5 is configured to enable the first heat exchange medium and the second heat exchange medium to exchange heat to provide heat for the first heat exchanger. The evaporator 8 is connected to the steam condensate tank 4, and the liquid after the steam discharged from the distillation tower 1 is heat-exchanged by the evaporator 8 enters the steam condensate tank 4. The first heat exchange medium is configured to provide heat for the falling film evaporator 2, so that the water in the hydrogen peroxide in the first channel is converted into steam and passed into the distillation tower 1 to achieve the concentration of the hydrogen peroxide. In this specific embodiment, the heat of the first heat exchange medium is transferred to the second heat exchange circuit through the condenser 5, and the second heat exchange circuit transfers the heat to the second channel of the falling film evaporator 2 to evaporate the water in the first channel to achieve the concentration of the hydrogen peroxide; the evaporator 8 is configured to enable the steam discharged from the distillation tower 1 to exchange heat with the first heat exchange medium, so that the first heat exchange medium evaporates back into the compressor 10, the pressure drop of the water vapor in the condenser 5 needs to be less than 5kPa, and the heat exchanger type of the condenser 5 can be BXM, BKU, BKM, or falling film evaporator.

[0055] The non-condensable gas of the distillation tower 1 after heat exchange in the evaporator 8 and the non-condensable gas of the falling film evaporator are extracted through the vacuum pump 9; the two sides of the vacuum pump 9 are also connected to the two ends of the pressure regulating branch, and the pressure regulating branch is configured to control the pressure and temperature of the top part of the distillation tower 1 by controlling the vacuum pump 9; the pressure range of the top part of the distillation tower 1 is 6-10kPaA, and the temperature is 36-46°C.

[0056] The first channel is also provided with a liquid level control branch connected thereto, and a liquid level control valve is provided on the liquid level control branch, and the liquid level control valve is configured to control the amount of hydrogen peroxide in the first channel by adjusting the feed amount of dilute hydrogen peroxide; the first channel is also provided with a temperature control branch connected thereto, and a temperature control valve is provided on the temperature control branch, and the temperature control valve is configured to control the temperature of hydrogen peroxide in the first channel by adjusting the discharge amount of concentrated hydrogen peroxide.

[0057] The temperature of the hydrogen peroxide in the first channel is 55-65° C., and the pressure is 8-12 kPaA; and / or the temperature of the steam generated in the second channel is 65-75° C., and the pressure is 25-35 kPaA.

[0058] The condensation temperature of the first heat exchange medium is 75-85°C, and the evaporation temperature is 25-35°C; preferably, the first heat exchange medium can be one or more of n-butane, isobutane, R134a, R245fa, ammonia, and propylene, but not limited thereto, as long as the condensation temperature of the first heat exchange medium is 75-85°C, and the evaporation temperature is 25-35°C, that is, it can meet the heat supply demand of the hydrogen peroxide in the first channel of the falling film heat exchanger 2, and those skilled in the art can set it according to actual conditions. In this specific embodiment, the second heat exchange medium is water. Of course, the specific type of the second heat exchange medium is not restrictive, and those skilled in the art can set it according to actual conditions.

[0059] A flow meter is provided at the outlet of the compressor 10 to detect the condensation amount of the heat-taking medium in the condenser 5. The compressor 10 is driven by a motor; a pressure control valve is provided at the inlet of the compressor 10, and the compressor 10 is provided with a reflux valve. The temperature, pressure and flow of the heat-taking medium at the outlet of the compressor 10 are adjusted by adjusting the pressure control valve and the reflux valve at the inlet of the compressor 10.

[0060] The compressor 10 is also connected to a gas-liquid separation member 11 .

[0061] Working principle:

[0062] The heat extracting medium evaporates in the evaporator 8, enters the gas-liquid separation component 11 for separation, and then enters the compressor 10 for compression. The compressed heat extracting medium enters the condenser 5 for condensation, and then enters the heat extracting medium storage tank 7, and then enters the evaporator 8 for evaporation. The steam condensate is sent to the condenser 5 by the steam condensate feed pump 6 for gasification, and then enters the second channel of the falling film evaporator 2 to provide a heat source, and enters the steam condensate tank 4 after condensation. The falling film evaporator 2 is provided with a hydrogen peroxide circulation pump 3, and a rare hydrogen peroxide feed and a concentrated hydrogen peroxide discharge are arranged on the circulation pipeline. The first channel of the falling film evaporator 2 generates steam and enters the distillation tower 1. There is pure water feed at the top of the distillation tower 1, concentrated hydrogen peroxide is produced at the bottom of the tower, and water vapor produced at the top of the tower enters the evaporator 8, and enters the steam condensate tank 4 after condensation. The non-condensable gas of the distillation tower 1 after condensation in the evaporator 8 and the non-condensable gas in the second channel of the falling film evaporator 2 are discharged through the vacuum pump 9.

[0063] The implementation results show that the power consumption for producing one ton of concentrated hydrogen peroxide is 255 to 270 kW. Based on an electricity price of 0.5 yuan per kWh, the energy consumption cost for producing one ton of concentrated hydrogen peroxide is 127.5 to 135 yuan. Compared with the existing hydrogen peroxide concentration devices on the market that use fresh steam as a heat source, the energy consumption cost for producing one ton of concentrated hydrogen peroxide is reduced by about 28% to 32%.

[0064] Comparative Example 1

[0065] like Figure 3As shown, a hydrogen peroxide concentration system comprises a distillation tower 1, a falling film evaporator 2, a steam condensate tank 4, a vacuum pump 9, a steam ejector 12, and a tower top condenser 13; the hydrogen peroxide outlet at the bottom of the falling film evaporator 2 is connected to the hydrogen peroxide inlet at the top of the falling film evaporator 2 through a circulation pipeline, the circulation pipeline is provided with a rare hydrogen peroxide feed port and a concentrated hydrogen peroxide discharge port, the circulation pipeline is also provided with a hydrogen peroxide circulation pump 3, the steam generated by the first channel of the falling film evaporator 2 enters the distillation tower 1; the steam outlet at the top of the distillation tower 1 is connected to the steam ejector 12 inlet; the fresh steam The steam enters the steam ejector 12, mixes with the top steam of the distillation tower 1, and then enters the steam inlet of the falling film evaporator 2; the condensate outlet of the falling film evaporator 2 is connected to the steam condensate tank 4; the steam outlet at the top of the distillation tower 1 is connected to the top condenser 13, and the top steam of the distillation tower 1 exchanges heat with the circulating cooling water in the top condenser 13, and the top condenser 13 is also connected to the steam condensate tank 4, and the top steam of the distillation tower 1 condenses and enters the steam condensate tank 4; the non-condensable gas at the top of the distillation tower 1 and the non-condensable gas in the second channel of the falling film evaporator 2 are discharged through the vacuum pump 9.

[0066] The distillation tower 1 is also provided with a pressure gauge, and the pressure range of the distillation tower 1 is controlled to be 6-10 kPaA and the pressure temperature to be 36-46° C. by adjusting the bypass pressure regulating valve of the vacuum pump 9.

[0067] A liquid level control circuit is also provided at the bottom of the falling film evaporator 2, and a falling film evaporator liquid level control valve is provided at the feed port of rare hydrogen peroxide, and the hydrogen peroxide liquid level is controlled by adjusting the feed amount of rare hydrogen peroxide; a temperature control circuit is provided at the bottom of the falling film evaporator 2, and a falling film evaporator temperature control valve is provided at the discharge port of concentrated hydrogen peroxide, and the hydrogen peroxide temperature is controlled by adjusting the discharge amount of concentrated hydrogen peroxide.

[0068] The temperature of hydrogen peroxide in falling film evaporator 2 is 55-65°C and the pressure is 8-12 kPaA; the temperature of water vapor in falling film evaporator 82 is 65-75°C and the pressure is 25-35 kPaA.

[0069] The pressure drop of water vapor in the top condenser of the tower needs to be less than 3kPa.

[0070] Working principle:

[0071] Fresh steam is mixed with the steam at the top of the distillation tower 1 through the steam ejector 12, and then enters the second channel of the falling film evaporator 2 to exchange heat with the hydrogen peroxide in the first channel, and enters the steam condensate tank 4 after condensation. The falling film evaporator 2 is provided with a hydrogen peroxide circulation pump 3, and a rare hydrogen peroxide feed and a concentrated hydrogen peroxide discharge are arranged on the circulation pipeline. The first channel of the falling film evaporator 2 generates steam and enters the distillation tower 1. The top of the distillation tower 1 has pure water feed, concentrated hydrogen peroxide is produced at the bottom of the tower, and the water vapor produced at the top of the tower enters the top condenser 13 to exchange heat with the circulating cooling water, and enters the steam condensate tank 4 after condensation. The non-condensable gas generated at the top of the distillation tower 1 and the non-condensable gas in the second channel of the falling film evaporator 2 are discharged through the vacuum pump 9.

[0072] The results show that the fresh steam consumption for producing each ton of concentrated hydrogen peroxide is 0.8 to 0.9 t. Based on the fresh steam price of 220 yuan / t, the energy consumption cost for producing each ton of concentrated hydrogen peroxide is 176 to 198 yuan.

[0073] By comparing the comparative examples and the embodiments, it can be seen that the hydrogen peroxide concentration system described in the utility model can significantly reduce energy consumption and save production costs in the hydrogen peroxide concentration process.

[0074] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A hydrogen peroxide concentration system, characterized in that: It comprises a distillation device, a first heat exchanger and a heat supply heat pump device, wherein the first heat exchanger is used for concentrating hydrogen peroxide; The first heat exchanger comprises a first channel and a second channel, hydrogen peroxide flows in the first channel, and a heat exchange medium capable of exchanging heat with hydrogen peroxide flows in the second channel; The heat supply heat pump device comprises a first heat exchange circuit, a first heat exchange medium flows in the first heat exchange circuit, a heat extraction medium storage component, a compressor and a second heat exchanger are arranged on the first heat exchange circuit, the heat extraction medium storage component can store the first heat exchange medium, the second heat exchanger is arranged between the heat extraction medium storage component and the compressor, and the distillation device is connected to the second heat exchanger; The first heat exchange medium is configured to provide heat to the first heat exchanger, so that the water in the hydrogen peroxide in the first channel is converted into steam and passed into the distillation device to achieve concentration of the hydrogen peroxide. The second heat exchanger is configured to enable the steam discharged from the distillation device to exchange heat with the first heat exchange medium, so that the first heat exchange medium evaporates back into the compressor.

2. The hydrogen peroxide concentration system according to claim 1, characterized in that: The first heat exchange circuit is connected to the second channel, one end of the second channel is connected to the exhaust port of the compressor, and the other end of the second channel is connected to the heat extraction medium storage component.

3. The hydrogen peroxide concentration system according to claim 1, characterized in that: The first heat exchange circuit is also provided with a third heat exchanger, and the third heat exchanger is provided between the exhaust port of the compressor and the heat extracting medium storage component; The heat supply heat pump device further comprises a second heat exchange circuit, a second heat exchange medium flows in the second heat exchange circuit, and the third heat exchanger and the steam condensate tank are arranged on the second heat exchange circuit; The second channel is connected to the second heat exchange circuit, one end of the second channel is connected to the third heat exchanger, and the other end of the second channel is connected to the steam condensate tank; The third heat exchanger is configured to enable the first heat exchange medium to exchange heat with the second heat exchange medium to provide heat for the first heat exchanger.

4. The hydrogen peroxide concentration system according to claim 3, characterized in that: The second heat exchanger is connected to the steam condensate tank, and the liquid after the steam discharged from the distillation device is heat-exchanged by the second heat exchanger enters the steam condensate tank.

5. The hydrogen peroxide concentration system according to claim 3, characterized in that: It also includes a vacuum pump, through which the non-condensable gas of the rectification device after heat exchange in the second heat exchanger and the non-condensable gas of the first heat exchanger are extracted.

6. The hydrogen peroxide concentration system according to claim 2, characterized in that: It also includes a vacuum pump, through which the non-condensable gas of the rectification device after heat exchange in the second heat exchanger is pumped out.

7. The hydrogen peroxide concentration system according to claim 1, characterized in that: The invention also includes a liquid level control branch connected to the first channel, wherein a liquid level control valve is provided on the liquid level control branch, and the liquid level control valve is configured to control the amount of hydrogen peroxide in the first channel by adjusting the feed amount of dilute hydrogen peroxide; and / or further includes a temperature control branch connected to the first channel, wherein a temperature control valve is provided on the temperature control branch, and the temperature control valve is configured to control the temperature of hydrogen peroxide in the first channel by adjusting the discharge amount of concentrated hydrogen peroxide.

8. The hydrogen peroxide concentration system according to claim 5 or 6, characterized in that: It also includes a pressure regulating branch, the two ends of which are connected to the two sides of the vacuum pump, and the pressure regulating branch is configured to control the pressure and temperature of the top part of the tower of the distillation device by controlling the vacuum pump.

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