Zero emission device for oxidized tail gas in production of hydrogen peroxide by anthraquinone process

Abstract

The utility model discloses an anthraquinone process hydrogen peroxide production oxidation tail gas zero emission device, which relates to the technical field of anthraquinone process hydrogen peroxide production, and comprises a hydrogen peroxide oxidation tail gas pipeline connected with a tail gas pressurization circulation unit through a triple cooling heavy aromatics recovery unit, and the triple cooling heavy aromatic hydrocarbon recovery unit comprises a tail gas condensation aromatic hydrocarbon recovery part, a main cold aromatic hydrocarbon recovery part and an expansion refrigeration aromatic hydrocarbon recovery part. The device has the beneficial effects that most of heavy aromatics in the oxidized tail gas are recovered by adopting triple cooling and triple separation, so that the purpose of saving energy consumption is achieved; and meanwhile, the differential pressure energy of the oxidized tail gas is recovered and converted into kinetic energy to drive an oxygen compressor to operate by adopting an expansion refrigeration aromatic hydrocarbon recovery part, and the recovery efficiency of aromatic hydrocarbon is improved by utilizing the cold energy of pressure expansion.

Description

Technical Field

[0001] The utility model relates to the technical field of anthraquinone process hydrogen peroxide production, and specifically, to an oxidation tail gas zero-emission device for anthraquinone process hydrogen peroxide production. Background Technique

[0002] In the oxidation process of anthraquinone process hydrogen peroxide production, the hydrogenated liquid contacts with air in the oxidation tower to carry out an oxidation reaction. Specifically, fresh pure oxygen is introduced from the bottom of the oxidation tower, and the hydrogenated liquid enters from the upper part of the oxidation tower. The liquid flows downward by the position difference, passes through multiple sieve plates for folding back and downward to carry out countercurrent contact reaction with the pure oxygen from the bottom, and gas-liquid separation is carried out at the top of the tower. The oxidation tail gas is discharged from the top of the tower, and the outlet pressure is about 0.20 MpaG. The main components in the oxidation tail gas are nitrogen, oxygen, heavy aromatic hydrocarbons, water, etc.

[0003] At present, the traditional treatment method for oxidation tail gas is to recover the pressure difference energy of the oxidation tail gas by using an expander, and then recover the heavy aromatic hydrocarbons by using the carbon particle adsorption method; this method has the following defects:

[0004] 1. Adsorbents are used;

[0005] 2. The operation of the carbon particle unit wastes a large amount of energy;

[0006] 3. A large amount of hazardous waste is generated.

[0007] For the problems in the related technology, no effective solution has been proposed yet. Content of the Utility Model

[0008] Aiming at the problems in the related technology, the purpose of the utility model is to propose an oxidation tail gas zero-emission device for anthraquinone process hydrogen peroxide production to overcome the above-mentioned technical problems existing in the existing related technology.

[0009] The technical solution of the utility model is realized as follows:

[0010] An oxidation tail gas zero-emission device for anthraquinone process hydrogen peroxide production, comprising: a hydrogen peroxide oxidation tail gas pipeline, the hydrogen peroxide oxidation tail gas pipeline is connected to a tail gas pressurization and circulation unit through a triple cooling and heavy aromatic hydrocarbon recovery unit, and the triple cooling and heavy aromatic hydrocarbon recovery unit includes: a tail gas condensation and aromatic hydrocarbon recovery part, a main cooling and aromatic hydrocarbon recovery part, and an expansion refrigeration and aromatic hydrocarbon recovery part, wherein;

[0011] The gas-phase outlet of the tail gas condensation aromatics recovery section is connected to the cooling channel of the main cooling aromatics recovery section. The gas-phase outlet of the main cooling aromatics recovery section is connected to the expansion refrigeration aromatics recovery section. The expansion refrigeration aromatics recovery section is connected to the heating channel of the main cooling aromatics recovery section. Moreover, the liquid-phase outlets of the gas condenser aromatics recovery section, the main cooling aromatics recovery section, and the expansion refrigeration aromatics recovery section are connected to the aromatics recovery tank.

[0012] Furthermore, the tail gas condensation aromatics recovery section includes a tail gas condenser and a tail gas condensate receiving tank, where;

[0013] The hydrogen peroxide oxidation tail gas pipeline is connected to the tail gas condensate receiving tank through the cooling channel of the tail gas condenser. The gas-phase outlet of the tail gas condensate receiving tank is connected to the main cooling aromatics recovery section. The liquid-phase outlet of the tail gas condensate receiving tank is connected to the aromatics recovery tank.

[0014] Furthermore, a first regulating valve is provided between the liquid-phase outlet of the tail gas condensate receiving tank and the aromatics recovery tank.

[0015] Furthermore, the main cooling aromatics recovery section includes a main cooling box and a second tail gas recovery tank, where;

[0016] The gas-phase outlet of the tail gas condensate receiving tank is connected to the second tail gas recovery tank through the cooling channel of the main cooling box. The gas-phase outlet of the second tail gas recovery tank is connected to the expansion refrigeration aromatics recovery section. The liquid-phase outlet of the second tail gas recovery tank is connected to the aromatics recovery tank.

[0017] Furthermore, a second regulating valve is provided between the liquid-phase outlet of the second tail gas recovery tank and the aromatics recovery tank.

[0018] Furthermore, the expansion refrigeration aromatics recovery section includes an expansion refrigerating machine, where;

[0019] The outlet of the expansion refrigerating machine is connected to the first tail gas recovery tank. The gas-phase outlet of the first tail gas recovery tank is connected to the tail gas pressurization and circulation unit through the heating channel of the main cooling box. The liquid-phase outlet of the first tail gas recovery tank is connected to the aromatics recovery tank.

[0020] Furthermore, a third regulating valve is provided between the liquid-phase outlet of the first tail gas recovery tank and the aromatics recovery tank.

[0021] Furthermore, the tail gas pressurization and circulation unit includes an oxygen compressor, an oxygen separator, and an oxidation tower, where;

[0022] The gas outlet of the oxygen compressor is connected to the oxidation tower through the oxygen separator, and the gas-phase outlet of the oxidation tower is connected to the tail gas condenser through the hydrogen peroxide oxidation tail gas pipeline.

[0023] Further, a fourth regulating valve is provided between the gas outlet of the oxygen compressor and the oxygen separator.

[0024] Further, a fifth regulating valve is provided between the gas-phase outlet of the oxidation tower and the tail gas condenser.

[0025] Advantages of the present utility model:

[0026] The present utility model realizes the recovery of most of the heavy aromatics in the oxidation tail gas by adopting triple temperature reduction and triple separation, so as to achieve the purpose of saving energy consumption; at the same time, the differential pressure energy of the oxidation tail gas is recovered by adopting the expansion refrigeration aromatics recovery part, which is converted into kinetic energy to drive the operation of the oxygen compressor, and the cold energy of pressure expansion is used to improve the recovery efficiency of aromatics. At the same time, the tail gas of the three-time recovery of aromatics is also used to cool and condense the oxidation tail gas in the hydrogen peroxide oxidation tail gas pipeline, so as to achieve the purpose of improving the recovery efficiency of aromatics in the main cold aromatics recovery part.

[0027] Other features and advantages of the present utility model will be described in the subsequent specification, and part of them will become obvious from the specification, or will be understood by implementing the present utility model. The purpose and other advantages of the present utility model are realized and obtained by the structure specifically pointed out in the specification and the drawings.

[0028] In order to make the above-mentioned purposes, features and advantages of the present utility model more obvious and understandable, the following specifically gives preferred embodiments and, in conjunction with the accompanying drawings, the detailed description is as follows. Description of the Drawings

[0029] In order to more clearly illustrate the technical solutions in the embodiments of the present utility model or the prior art, the following will briefly introduce the drawings required to be used in the embodiments. Obviously, the following-described drawings are only some embodiments of the present utility model. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0030] Figure 1 It is a principle block diagram of an oxidation tail gas zero-emission device for anthraquinone method hydrogen peroxide production according to an embodiment of the present utility model.

[0031] In the figure:

[0032] 1. Hydrogen peroxide oxidation tail gas pipeline; 2. Tail gas condenser; 3. Tail gas condensate receiving tank; 4. Main cold box; 5. Second tail gas recovery tank; 6. Expansion refrigerator; 7. First tail gas recovery tank; 8. Oxygen compressor; 9. Oxygen separator; 10. Oxidation tower; 11. Aromatic hydrocarbon recovery tank; 12. First regulating valve; 13. Second regulating valve; 14. Third regulating valve; 15. Fourth regulating valve; 16. Fifth regulating valve. Detailed implementation manners

[0033] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. Apparently, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention shall fall within the protection scope of the present invention.

[0034] According to an embodiment of the present invention, there is provided an oxidation tail gas zero-emission device for anthraquinone process hydrogen peroxide production.

[0035] As Figure 1 shown, an oxidation tail gas zero-emission device for anthraquinone process hydrogen peroxide production includes: a hydrogen peroxide oxidation tail gas pipeline 1, and the hydrogen peroxide oxidation tail gas pipeline 1 is connected to a tail gas pressurization and circulation unit through a triple cooling and heavy aromatic hydrocarbon recovery unit. The triple cooling and heavy aromatic hydrocarbon recovery unit includes: a tail gas condensation aromatic hydrocarbon recovery part, a main cold aromatic hydrocarbon recovery part, and an expansion refrigeration aromatic hydrocarbon recovery part, wherein;

[0036] The gas phase outlet of the tail gas condensation aromatic hydrocarbon recovery part is connected to the cooling channel of the main cold aromatic hydrocarbon recovery part. The gas phase outlet of the main cold aromatic hydrocarbon recovery part is connected to the expansion refrigeration aromatic hydrocarbon recovery part. The expansion refrigeration aromatic hydrocarbon recovery part is connected to the heating channel of the main cold aromatic hydrocarbon recovery part. And the liquid phase outlets of the gas condenser aromatic hydrocarbon recovery part, the main cold aromatic hydrocarbon recovery part, and the expansion refrigeration aromatic hydrocarbon recovery part are connected to the aromatic hydrocarbon recovery tank 11.

[0037] In addition, the tail gas condensation aromatic hydrocarbon recovery part includes: a tail gas condenser 2 and a tail gas condensate receiving tank 3, wherein;

[0038] The hydrogen peroxide oxidation tail gas pipeline 1 is connected to the tail gas condensate receiving tank 3 through the cooling channel of the tail gas condenser 2. The gas phase outlet of the tail gas condensate receiving tank 3 is connected to the main cold aromatic hydrocarbon recovery part. The liquid phase outlet of the tail gas condensate receiving tank 3 is connected to the aromatic hydrocarbon recovery tank 11.

[0039] Wherein, a first regulating valve 12 is provided between the liquid phase outlet of the tail gas condensate receiving tank 3 and the aromatic hydrocarbon recovery tank 11.

[0040] In addition, the main cold aromatic hydrocarbon recovery part includes: a main cold box 4 and a second tail gas recovery tank 5, wherein;

[0041] The gas-phase outlet of the tail gas condensate receiver tank 3 is connected to the second tail gas recovery tank 5 through the temperature reduction channel of the main cold box 4. The gas-phase outlet of the second tail gas recovery tank 5 is connected to the expansion refrigeration aromatic hydrocarbon recovery section. The liquid-phase outlet of the second tail gas recovery tank 5 is connected to the aromatic hydrocarbon recovery tank 11.

[0042] Wherein, a second regulating valve 13 is provided between the liquid-phase outlet of the second tail gas recovery tank 5 and the aromatic hydrocarbon recovery tank 11.

[0043] In addition, the expansion refrigeration aromatic hydrocarbon recovery section includes: an expansion refrigerating machine 6, wherein;

[0044] The outlet of the expansion refrigerating machine 6 is connected to the first tail gas recovery tank 7. The gas-phase outlet of the first tail gas recovery tank 7 is connected to the tail gas pressurization and circulation unit through the temperature increase channel of the main cold box 4. The liquid-phase outlet of the first tail gas recovery tank 7 is connected to the aromatic hydrocarbon recovery tank 11.

[0045] Wherein, a third regulating valve 14 is provided between the liquid-phase outlet of the first tail gas recovery tank 7 and the aromatic hydrocarbon recovery tank 11.

[0046] In addition, the tail gas pressurization and circulation unit includes: an oxygen compressor 8, an oxygen separator 9 and an oxidation tower 10, wherein;

[0047] The gas outlet of the oxygen compressor 8 is connected to the oxidation tower 10 through the oxygen separator 9. The gas-phase outlet of the oxidation tower 10 is connected to the tail gas condenser 2 through the hydrogen peroxide oxidation tail gas pipeline 1.

[0048] Wherein, a fourth regulating valve 15 is provided between the gas outlet of the oxygen compressor 8 and the oxygen separator 9. A fifth regulating valve 16 is provided between the gas-phase outlet of the oxidation tower 10 and the tail gas condenser 2.

[0049] By means of the above solution, most of the heavy aromatic hydrocarbons in the oxidation tail gas are recovered by adopting triple temperature reduction and triple separation to achieve the purpose of saving energy consumption. At the same time, the differential pressure energy of the oxidation tail gas is recovered by adopting the expansion refrigeration aromatic hydrocarbon recovery section, which is converted into kinetic energy to drive the operation of the oxygen compressor 8, and the cold energy of pressure expansion is used to improve the recovery efficiency of aromatic hydrocarbons. At the same time, the tail gas with three-time recovered aromatic hydrocarbons is also used to cool and condense the oxidation tail gas in the hydrogen peroxide oxidation tail gas pipeline 1 to achieve the purpose of improving the recovery efficiency of aromatic hydrocarbons in the main cold aromatic hydrocarbon recovery section.

[0050] For the above-mentioned oxygen compressor 8 in this technical solution, the power of the oxygen compressor 8 comes from the recovery and utilization of the differential pressure energy of the oxidation tail gas by the expansion refrigeration aromatic hydrocarbon recovery section, and no electric energy is required. Since the oxidation tail gas is recycled, the carbon particle adsorption unit is completely cancelled, the adsorbent is no longer used, the generation of hazardous waste is reduced, a large amount of energy is saved, and at the same time, the environmental protection pressure of the oxidation tail gas is greatly reduced.

[0051] Specifically, the following steps are adopted to treat the oxidation tail gas of hydrogen peroxide, as follows:

[0052] Step S1, the oxidation tail gas in the hydrogen peroxide oxidation tail gas pipeline 1 enters the cooling channel of the tail gas condenser 2 for cooling; the oxidation tail gas comes from the gas phase outlet of the oxidation tower 10. The temperature of the oxidation tail gas in the hydrogen peroxide oxidation tail gas pipeline 1 is 35 - 50°C, and the pressure is 0.2 - 0.3 MpaG; the temperature of the oxidation tail gas after passing through the cooling channel is 35 - 40°C;

[0053] Step S2, the cooled oxidation tail gas enters the tail gas condensate receiving tank 3 for gas-liquid separation. The liquid phase after gas-liquid separation enters the aromatic hydrocarbon recovery tank 11 through the first regulating valve 12 for recovery, and the gas phase after gas-liquid separation enters the cooling channel of the main cold box 4 for heat exchange; the temperature of the oxidation tail gas after passing through the cooling channel is 30 - 35°C;

[0054] Step S3, the cooled oxidation tail gas enters the second tail gas recovery tank 5 for gas-liquid separation. The liquid phase after gas-liquid separation enters the aromatic hydrocarbon recovery tank 11 through the second regulating valve 13 for recovery, and the gas phase after gas-liquid separation enters the expansion refrigerating machine 6 to convert potential energy into kinetic energy and then drive the oxygen compressor 8 to operate; at this time, the pressure of the oxidation tail gas at the outlet of the expansion refrigerating machine 6 is 10 - 17 kpaG, and the temperature is 0 - 5°C;

[0055] Step S4, the oxidation tail gas cooled by the expansion refrigerating machine 6 enters the first tail gas recovery tank 7 for gas-liquid separation, and the condensed aromatic hydrocarbons enter the aromatic hydrocarbon recovery tank 11 through the third regulating valve 14 for recovery;

[0056] Step S5, the gas phase from the first tail gas recovery tank 7 exchanges heat with the cooling process through the heating channel of the main cold box 4, and after heat exchange, it enters the oxygen compressor 8; the temperature of the expanded gas after passing through the heating channel of the main cold box 4 is 30 - 35°C;

[0057] Step S6, the tail gas entering the oxygen compressor 8 is pressurized and then enters the oxygen separator 9 for gas-liquid separation, and then enters the oxidation tower 10 through the fourth regulating valve 15;

[0058] Step S7, the unreacted oxidation tail gas passes through the gas phase outlet of the oxidation tower 10 and enters the cooling channel of the tail gas condenser 2 through the fifth regulating valve 16, thus completing a cycle.

[0059] In addition, it should be particularly noted that after the implementation of the present utility model, there will be no power consumption and steam consumption, and it is more energy-saving; no adsorbent is used, reducing the generation of hazardous waste; the oxidation tail gas is zero-emission, does not generate VOCs, and does not pollute the environment. It not only has obvious economic benefits but also remarkable environmental protection effects.

[0060] In summary, by means of the above technical solutions of the present utility model, the following effects can be achieved: most of the heavy aromatics in the oxidation tail gas can be recovered by adopting triple cooling and triple separation, so as to achieve the purpose of saving energy consumption; at the same time, the differential pressure energy of the oxidation tail gas is recovered by the expansion refrigeration aromatics recovery part, converted into kinetic energy to drive the operation of the oxygen compressor 8, and the cold energy of pressure expansion is used to improve the aromatics recovery efficiency. At the same time, the tail gas of the three - time aromatics recovery is also used to cool and condense the oxidation tail gas from the hydrogen peroxide oxidation tail gas pipeline 1, so as to achieve the purpose of improving the aromatics recovery efficiency of the main cold aromatics recovery part.

[0061] The above are only the preferred embodiments of the present utility model and are not intended to limit the present utility model. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present utility model shall be included in the protection scope of the present utility model.

Claims

1. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device, characterized in that, Comprising: The hydrogen peroxide oxidation tail gas pipeline (1), the hydrogen peroxide oxidation tail gas pipeline (1) is connected to the tail gas pressurization and circulation unit through a triple cooling heavy aromatic hydrocarbon recovery unit, and the triple cooling heavy aromatic hydrocarbon recovery unit includes: a tail gas condensation aromatic hydrocarbon recovery part, a main cooling aromatic hydrocarbon recovery part, and an expansion refrigeration aromatic hydrocarbon recovery part, wherein; The gas phase outlet of the tail gas condensation aromatic hydrocarbon recovery part is connected to the cooling channel of the main cooling aromatic hydrocarbon recovery part, the gas phase outlet of the main cooling aromatic hydrocarbon recovery part is connected to the expansion refrigeration aromatic hydrocarbon recovery part, the expansion refrigeration aromatic hydrocarbon recovery part is connected to the heating channel of the main cooling aromatic hydrocarbon recovery part, and the liquid phase outlets of the tail gas condenser aromatic hydrocarbon recovery part, the main cooling aromatic hydrocarbon recovery part, and the expansion refrigeration aromatic hydrocarbon recovery part are connected to the aromatic hydrocarbon recovery tank (11).

2. The zero-emission device for oxidation tail gas in anthraquinone process hydrogen peroxide production according to claim 1, characterized in that, The tail gas condensation aromatic hydrocarbon recovery part includes: a tail gas condenser (2) and a tail gas condensate receiving tank (3), wherein; The hydrogen peroxide oxidation tail gas pipeline (1) is connected to the tail gas condensate receiving tank (3) through the cooling channel of the tail gas condenser (2), the gas phase outlet of the tail gas condensate receiving tank (3) is connected to the main cooling aromatic hydrocarbon recovery part, and the liquid phase outlet of the tail gas condensate receiving tank (3) is connected to the aromatic hydrocarbon recovery tank (11).

3. The zero-emission device for oxidation tail gas in anthraquinone process hydrogen peroxide production according to claim 2, characterized in that, A first regulating valve (12) is provided between the liquid phase outlet of the tail gas condensate receiving tank (3) and the aromatic hydrocarbon recovery tank (11).

4. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 2, characterized in that, The main cooling aromatic hydrocarbon recovery part includes: a main cooling box (4) and a second tail gas recovery tank (5), wherein; The gas phase outlet of the tail gas condensate receiving tank (3) is connected to the second tail gas recovery tank (5) through the cooling channel of the main cooling box (4), the gas phase outlet of the second tail gas recovery tank (5) is connected to the expansion refrigeration aromatic hydrocarbon recovery part, and the liquid phase outlet of the second tail gas recovery tank (5) is connected to the aromatic hydrocarbon recovery tank (11).

5. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 4, characterized in that, A second regulating valve (13) is provided between the liquid phase outlet of the second tail gas recovery tank (5) and the aromatic hydrocarbon recovery tank (11).

6. The zero-emission device for the oxidation tail gas in the production of hydrogen peroxide by the anthraquinone method according to claim 4, characterized in that, The expansion refrigeration aromatic hydrocarbon recovery part includes: an expansion refrigeration machine (6), wherein; The outlet of the expansion refrigeration machine (6) is connected to the first tail gas recovery tank (7), the gas phase outlet of the first tail gas recovery tank (7) is connected to the tail gas pressurization and circulation unit through the heating channel of the main cooling box (4), and the liquid phase outlet of the first tail gas recovery tank (7) is connected to the aromatic hydrocarbon recovery tank (11).

7. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 6, characterized in that, A third regulating valve (14) is provided between the liquid phase outlet of the first tail gas recovery tank (7) and the aromatic hydrocarbon recovery tank (11).

8. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 2, characterized in that, The tail gas pressurization and circulation unit includes: an oxygen compressor (8), an oxygen separator (9), and an oxidation tower (10), wherein; The gas outlet of the oxygen compressor (8) is connected to the oxidation tower (10) through the oxygen separator (9), and the gas phase outlet of the oxidation tower (10) is connected to the tail gas condenser (2) through the hydrogen peroxide oxidation tail gas pipeline (1).

9. An anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 8, characterized in that, A fourth regulating valve (15) is provided between the gas outlet of the oxygen compressor (8) and the oxygen separator (9).

10. The anthraquinone process hydrogen peroxide production oxidation tail gas zero-emission device according to claim 8, characterized in that, A fifth regulating valve (16) is provided between the gas-phase outlet of the oxidation tower (10) and the tail gas condenser (2).

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