CN210396833U - Trimellitic anhydride continuous production tail gas turbine energy recovery device - Google Patents
Trimellitic anhydride continuous production tail gas turbine energy recovery device Download PDFInfo
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Abstract
The utility model discloses a trimellitic anhydride continuous production tail gas turbine energy recuperation device in the energy-conserving technical field of chemical industry, including a heat transfer device, one-level turbine, secondary heat transfer device and second grade turbine, the one-level turbine includes one-level expander and one-level compressor, and the second grade turbine includes second grade expander and second grade compressor, one-level compressor, second grade compressor are used for the import that compressed air supplies oxidation reaction device, a heat transfer device's access connection oxidation reaction's tail gas pipeline, the import of a heat transfer device's exit linkage one-level expander, the import of the exit linkage secondary heat transfer device of one-level expander, the import of secondary heat transfer device's exit linkage second grade expander, the export switch-on exhaust chimney of second grade expander. The method solves the problem that the energy of the middle-low pressure tail gas generated in the production of the trimellitic anhydride is difficult to recover, and provides an energy-saving technical support for the large-scale industrial continuous production of the trimellitic anhydride.
Description
Technical Field
The utility model relates to a tail gas turbine energy recovery device produced by a trimellitic anhydride continuous method, in particular to an energy-saving process for driving a compressor by a tail gas turbine generated in a trimellitic anhydride continuous method oxidation process. Belongs to the technical field of chemical energy conservation.
Background
In the industrial production process, tail gas with certain pressure energy, kinetic energy and heat energy is often generated, and if the tail gas is directly discharged, not only energy is wasted, but also the environment is polluted. The technical principle of the industrial tail gas turbine energy recovery technology is that the tail gas expansion is utilized to convert pressure energy, kinetic energy and heat energy into mechanical energy to generate or drive, so that the purposes of energy conservation and environmental protection are achieved.
The energy recovery of the tail gas turbine in the Production of Terephthalic Acid (PTA) recovers the pressure energy, kinetic energy and heat energy of the tail gas generated in the reaction, provides the power consumption of a compressor unit together with the turbine, ensures the balance of the energy of the unit operation in the process, and simultaneously the tail gas turbine also plays the role of regulating the pressure of a device. The tail gas from the absorption tower is expanded in a tail gas turbine to do work after heat exchange, and then is incinerated and discharged to the atmosphere. The composition of the tail gas is roughly similar to that of the tail gas of a terephthalic acid plant, and mainly contains nitrogen, a small amount of carbon dioxide, oxygen and moisture, and some corrosive gases.
The process of recycling and utilizing the tail gas of 25 ten thousand tons of terephthalic acid produced every year at present is as follows: the high-temperature low-pressure high-pressure tail gas (mainly comprising nitrogen, the temperature is about 185 ℃, the pressure is about 1.0 MPa, and the flow is 8000 m) after the oxidation reaction3And/h) enters the air compressor unit for use after heat and energy are recycled. The compressor unit includes a steam turbine, a tail gas expander and an air compressor. Wherein the air compressor is composed of a steam turbine and an exhaust gasThe expansion is driven together, and the compressed air is used for the reaction of the oxidation unit. Tail gas with the temperature of 185 ℃ and the pressure of 0.96 MPa generated from the oxidation reactor sequentially passes through an oxidation tail gas condenser to respectively generate steam with the pressure of 0.4 MPa, 0.2 MPa and 0.07 MPa for a steam turbine to use; and simultaneously generates 0.34MPa steam which is used as heating steam of a solvent tower kettle of the device. The temperature of the tail gas after heat recovery is reduced to about 97 ℃, and the total amount is about 78000 m3And/h, the temperature of the liquid is controlled by controlling the liquid level. When the device is normally produced, the three-grade steam not only can meet the consumption required by the steam turbine and provide 70 percent of power (about 7600 kW) for the air compressor, but also the rest part can enter a pipe network to heat other pipelines, valves and equipment.
Trimellitic anhydride (TMA) is the main raw material for producing environment-friendly plasticizers and polyester resins. In the process of producing trimellitic anhydride by using a liquid-phase air method, when oxidation reaction is carried out in an oxidation tower, a large amount of organic matters (such as glacial acetic acid, trimellitic benzene and the like) are contained in waste gas generated at the top of the oxidation tower, and the waste gas rich in the organic matters is recovered by using an absorption tower and a water washing tower. Therefore, a large amount of water resource waste is caused, and meanwhile, certain pollution is caused to the environment. Meanwhile, the tail gas generated in the production of trimellitic anhydride belongs to low-temperature, medium-pressure and low-gas-content tail gas (the temperature is about 30 ℃, the pressure is about 2.0 MPa, and the flow is 1000 m)3Around/h). The tail gas also has huge energy which can be recovered and utilized. If the energy is directly discharged with tail gas under the treatment of any recovery measures, the pollution to the atmospheric environment can be caused, and the energy can be wasted. But the recovery of the medium-pressure low-gas tail gas generated in the production of trimellitic anhydride cannot be realized by directly adopting the existing PTA tail gas turbine energy recovery process.
The prior tail gas turbine energy recovery process for producing trimellitic anhydride is not reported, and the main problems are as follows: 1) the recovery of medium-pressure low-gas tail gas is difficult; 2) the tail gas turbine has low energy recovery efficiency and high economic cost; 3) the low gas content of the tail gas of the batch method is difficult to utilize.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a trimellitic anhydride continuous process production tail gas turbine energy recuperation device to the well low pressure tail gas energy that produces is difficult to the problem of retrieving in solving prior art trimellitic anhydride production, provides energy-conserving technical support for trimellitic anhydride's extensive industry continuous process production.
Therefore, the utility model discloses a trimellitic anhydride continuous process produces tail gas turbine energy recuperation device, including a heat transfer device, one-level turbine, secondary heat transfer device and second grade turbine, the one-level turbine includes the one-level compressor in one-level expander and one-level expander shaft area, and the second grade turbine includes the second grade compressor in second grade expander and second grade expander shaft area, one-level compressor, second grade compressor are used for compressed air to supply the import of oxidation reaction device, and a heat transfer device's access connection oxidation reaction's tail gas pipeline, the import of a heat transfer device's exit linkage one-level expander, the exit linkage secondary heat transfer device's of one-level expander import, the import of secondary heat transfer device's exit linkage second grade expander, the export switch-on exhaust chimney of second grade expander.
The utility model discloses when carrying out energy recuperation, carry out according to following step:
1) the reaction tail gas from the trimellitic anhydride oxidation reaction device is reacted at the temperature of 30-40 ℃ and the flow rate of 1000-1200 m3H, the pressure is 2.1-2.5 MPa; performing primary heat exchange to obtain gas with the temperature of 95-110 ℃ and the pressure of 2.1-2.5 MPa; the gas flow after primary heat exchange is 1300-1400 m3/h；
2) The gas after primary heat exchange is sent into an inlet of a primary expansion machine, the primary expansion machine applies work outwards through a primary compressor, the temperature of the gas at the outlet of the primary expansion machine is 45-55 ℃, and the pressure is 0.6-0.7 MPa; the outlet flow of the first-stage expansion machine is 3500-3600 m correspondingly3/h；
3) The temperature of the outlet gas of the primary expander is 95-150 ℃ and the pressure is 0.6-0.7 MPa after secondary heat exchange; after secondary heat exchange, the flow rate is 4400-3/h；
4) The gas after the secondary heat exchange is sent into an inlet of a secondary expansion machine, and the secondary expansion machine passes through a secondary compressorApplying work to the outside, wherein the temperature of the gas at the outlet of the secondary expansion machine is 30-35 ℃, and the pressure is 0.15-0.25 MPa; the outlet flow of the secondary expansion machine corresponds to 11000-3/h；
5) And the gas at the outlet of the secondary expansion machine is discharged outwards through an exhaust chimney.
In the process of producing trimellitic anhydride by a liquid-phase air oxidation method, trimellitic acid is prepared by oxidizing trimellitic benzene serving as a raw material, acetic acid serving as a solvent, soluble Co-Mn salt and bromide serving as catalysts by using air at 200 ℃ under the pressure of 2.0-2.3 MPa, and then trimellitic anhydride is generated by dehydration. After oxygen is consumed, tail gas mainly contains nitrogen and a small amount of carbon dioxide, the tail gas produced by trimellitic anhydride belongs to medium-pressure low-gas-content tail gas, and the recycling size of the tail gas mainly depends on the flow size of the tail gas and the problem of continuous gas supply. The beneficial effects of the utility model reside in that: the utility model discloses a heat transfer device and secondary heat transfer device have promoted the energy of tail gas, have promoted flow and pressure for the tail gas flow size accords with the requirement of the continuous air feed of one-level expander and second grade expander, thereby reaches the technical requirement of stable recovered energy. The recovered energy is sent into the oxidation reaction device by compressing the raw material air through the primary air compressor and the secondary air compressor, so that the purpose of improving the energy recovery and utilization efficiency is achieved. The method is suitable for recovering the tail gas energy in the production of the trimellitic anhydride by the liquid-phase air continuous oxidation method.
As the utility model discloses a further improvement lies in, a heat transfer device includes one-level nitrogen gas preheater and one-level steam heater, and one-level steam heater sets up between one-level nitrogen gas preheater and one-level expander. The primary steam heater serves as a supplementary heating device for insufficient temperature.
As the utility model discloses a further improvement lies in, secondary heat transfer device includes second grade nitrogen gas pre-heater, flue gas heater and second grade steam heater, second grade nitrogen gas pre-heater and flue gas heater be connected the import of back reconnection to the second grade expander with second grade steam heater after parallelly connected the setting again. The secondary heat exchange is carried out in a secondary nitrogen preheater, a flue gas heater and a secondary steam heater, wherein the secondary nitrogen preheater and the flue gas heater are arranged in parallel and then connected with the secondary steam heater and then connected to the inlet of a secondary expansion machine. The secondary steam heater serves as a supplementary heating device for insufficient temperature. The secondary nitrogen preheater and the flue gas heater can work in parallel or independently; when the parallel connection work is carried out, the optimal proportion of the recovered heat energy can be achieved by adjusting the distribution proportion of the air inlet flow of the tail gas.
The further improvement of the utility model is that the heat source ends of the primary nitrogen preheater and the secondary nitrogen preheater are connected with the flue gas of the oil furnace; the heat source of the flue gas heater is connected with the flue gas of the incinerator. The heat source of the primary nitrogen preheating and the secondary nitrogen preheating is from oil furnace flue gas generated after combustion of natural gas in the oil furnace; the heat source of the flue gas heater is generated by burning black slag separated from the tower bottom in the continuous production of the trimellitic anhydride by an incinerator. In the production process of trimellitic anhydride, natural gas is combusted through an oil furnace to supply heat so as to maintain the working temperature in the system, and the energy of the combusted flue gas can be used for improving the energy of tail gas; in addition, the black slag at the bottom of the tower contains a large amount of combustible organic matters, heat is generated by burning the black slag, and the heat can also improve the energy of tail gas through a flue gas heater and recover the energy in a secondary compressor. In order to further reduce energy consumption, the secondary heat exchange is preferentially heated by a flue gas heater, then heated by a secondary nitrogen preheater, and finally heated by a secondary steam heater. The latter carries out supplementary heating when the former heats the tail gas insufficiently to reach the best energy-saving effect.
As a further improvement of the utility model, two groups of primary steam heaters are connected in parallel with a primary turbine; two groups of secondary steam heaters and two groups of secondary turbines are also arranged in parallel. The one-on-one-standby mode can be realized to ensure continuous production.
In the utility model, a plurality of valves are arranged on pipelines among the related devices for switching, controlling flow, converting or realizing bypass control, and one part of tail gas after oxidation reaction and purification is controlled at 0.69 MPa by a pressure regulating valve and is used for installing a nitrogen pipe network, circulating nitrogen of a drier and a high-pressure air conveying system; and the other part of purified tail gas is heated in the primary nitrogen preheater and then enters the primary expansion machine to drive the primary compressor to do work under the control of the flow regulating valve. And the tail gas after primary expansion drives a secondary compressor to do work after secondary heat exchange. The expander provides 30% of power (about 3400 kW) for the compressor after secondary expansion. The heat and energy of the tail gas are utilized to drive the steam turbine and the expansion machine to do work, so that the externally introduced 1 MPa steam is reduced, the steam and the tail gas are utilized and recovered to the maximum extent, and the cost of the trimellitic anhydride product is greatly reduced. More specifically, the utility model has the advantages that:
1) and recovering the energy of the low-temperature low-gas tail gas generated in the TMA production process.
2) The energy of flue nitrogen of an incinerator or a natural gas furnace is utilized.
3) The energy-saving efficiency is 40-50%.
Drawings
Fig. 1 is a flow chart of the present invention.
Detailed Description
As shown in fig. 1, the turbine energy recovery device for tail gas produced by the continuous method of trimellitic anhydride comprises a primary heat exchange device, a primary turbine, a secondary heat exchange device and a secondary turbine, wherein the primary heat exchange device comprises a primary nitrogen preheater E303a, primary steam heaters H101a and H101b, and the primary steam heaters H101a and H101b are arranged between the primary nitrogen preheater E303a and primary expanders EXP1a and EXP1 b; the secondary heat exchange device comprises a secondary nitrogen preheater E303b, a flue gas heater E304 and secondary steam heaters H102a and H102b, wherein the secondary nitrogen preheater E303b and the flue gas heater E304 are arranged in parallel, then are connected with the secondary steam heaters H102a and H102b, and then are connected with inlets of secondary expanders EXP2a and EXP2 b; two groups of first-stage steam heaters H101a and H101b are connected with the first-stage turbine in parallel, and one group is used and the other group is prepared; two groups of secondary steam heaters H102a and H102b and a secondary turbine are also arranged in parallel, and one group is used and the other group is prepared; the heat source ends of the primary nitrogen preheater E303a and the secondary nitrogen preheater E303b are connected with the flue gas of the oil furnace; the heat source of the flue gas heater E304 is connected with the flue gas of the incinerator; the primary turbine comprises a primary expander EXP1a, an EXP1b and a primary compressor PR1a and PR1b of a primary expander shaft belt, the secondary turbine comprises a secondary expander EXP2a, an EXP2b and a secondary compressor PR2a and PR2b of a secondary expander shaft belt, the primary compressor PR1a, the PR1b, the secondary compressor PR2a and the PR2b are used for supplying compressed air to an inlet of an oxidation reaction device, an inlet of a primary heat exchange device is connected with a tail gas pipeline of the oxidation reaction, an outlet of the primary heat exchange device is connected with inlets of the primary expander EXP1a and the EXP1b, outlets of the primary expander EXP1a and the EXP1b are connected with inlets of a secondary heat exchange device, an outlet of the secondary heat exchange device is connected with inlets of the secondary expander EXP2a and the EXP2b, and outlets of the secondary expander EXP2a and the EXP2b are communicated with an exhaust chimney.
The working process comprises the following steps:
1) the temperature of the oxidation reaction tail gas from the trimellitic anhydride oxidation reaction device is 30-40 ℃, and the flow rate is 1000-3H, the pressure is 2.1-2.5 MPa; performing primary heat exchange to obtain gas with the temperature of 95-110 ℃ and the pressure of 2.1-2.5 MPa; the gas flow after primary heat exchange is 1300-1400 m3/h correspondingly; the primary heat exchange is carried out in a primary nitrogen preheater E303a and primary steam heaters H101a and H101b, wherein the primary steam heaters H101a and H101b are arranged between the primary nitrogen preheater E303a and primary expanders EXP1a and EXP1 b; the primary steam heaters H101a, H101b serve as supplementary heating devices with insufficient temperature.
2) The gas after primary heat exchange is sent into inlets of first-stage expanders EXP1a and EXP1b, the first-stage expanders EXP1a and EXP1b do work outwards through first-stage compressors PR1a and PR1b, the temperature of the gas at outlets of the first-stage expanders EXP1a and EXP1b is 45-55 ℃, and the pressure is 0.6-0.7 MPa; the outlet flow rates of the first-stage expansion machines EXP1a and EXP1b are 3500-3600 m3/h。
3) The temperature of the outlet gas of the first-stage expander EXP1a and EXP1b is 95-150 ℃ and the pressure is 0.6-0.7 MPa after secondary heat exchange; after secondary heat exchange, the flow rate is 4400-3H; the secondary heat exchange is carried out in a secondary nitrogen preheater E303b, a flue gas heater E304 and secondary steam heaters H102a and H102b, wherein the secondary nitrogen preheater E303b and the flue gas heater E304 are arranged in parallel, then are connected with the secondary steam heaters H102a and H102b, and then are connected with the secondary nitrogen preheaterInlets of expanders EXP2a, EXP2 b. The secondary steam heaters H102a, H102b act as supplementary heating devices with insufficient temperature. The heat sources of the primary nitrogen preheating E303a and the secondary nitrogen preheater E303b are from oil furnace flue gas generated after combustion of natural gas in the oil furnace; the heat source of the flue gas heater is generated by burning black slag separated from the tower bottom in the continuous production of the trimellitic anhydride by an incinerator. In the production process of trimellitic anhydride, natural gas is combusted through an oil furnace to supply heat so as to maintain the working temperature in the system, and the energy of the combusted flue gas can be used for improving the energy of tail gas; in addition, the black slag at the bottom of the tower contains a large amount of combustible organic matters, heat is generated through burning the black slag, and the heat can also improve the energy of tail gas through a flue gas heater.
4) The gas after secondary heat exchange is sent into inlets of secondary expanders EXP2a and EXP2b, the secondary expanders EXP2a and EXP2b do work outwards through secondary compressors PR2a and PR2b, the temperature of outlet gas of the secondary expanders EXP2a and EXP2b is 30-35 ℃, and the pressure is 0.15-0.25 MPa; the outlet flow rates of the two-stage expanders EXP2a and EXP2b are 11000-12000m3H; two sets of secondary steam heaters H102a, H102b and secondary expanders EXP2a, EXP2b are also provided in parallel.
5) And the gases at the outlets of the two-stage expanders EXP2a and EXP2b are discharged outwards through an exhaust chimney.
In order to further reduce energy consumption, the secondary heat exchange is preferably heated by a flue gas heater E304, then heated by a secondary nitrogen preheater E303b, and finally heated by secondary steam heaters H102a and H102 b. The latter carries out supplementary heating when the former heats the tail gas insufficiently to reach the best energy-saving effect.
The utility model discloses in, all be equipped with a plurality of valves on the pipeline between each equipment that involves and be used for switch, flow control, conversion or realize bypass control.
Specifically, the above method can be implemented by the following embodiments:
example 1:
oxidation reaction tail gas (30 ℃, 1000 m) of trimellitic anhydride device3H, 2.1 MPa) is firstly sent into a heat supply workshop and preheated by a primary nitrogen preheater E303a (95 ℃,1300 m3/H, 2.1 MPa) into the primary expander EXP1a or EXP1b, and when the temperature is insufficient, the heating is supplemented by the primary steam heaters H101a and H101 b. Exit gas (45 ℃ C., 3500 m) from first-stage expander EXP1a or EXP1b30.6 MPa) enters a flue gas heater E304 and a secondary nitrogen preheater E303b for heating, the flue gas heater E304 and the secondary nitrogen preheater E303b can work in parallel or independently, the ratio of the tail gas flow of the flue gas heater E304 and the tail gas flow of the secondary nitrogen preheater E303b can be adjusted when the flue gas heater E304 and the secondary nitrogen preheater are connected in parallel, and the heated tail gas (95 ℃, 4400 m) is obtained30.6 MPa) into secondary expander EXP2a or EXP2b, and when the temperature is insufficient, the heating is supplemented by secondary steam heaters H102a, H102 b. Tail gas (30 ℃, 11000 m) at the outlet of the secondary expander EXP2a and EXP2b3H, 0.15 MPa) can be directly discharged from an exhaust chimney. The beneficial effects are that: the energy-saving efficiency reaches 40 percent.
Example 2:
oxidation reaction tail gas (40 ℃, 1100 m) of trimellitic anhydride device3H, 2.3 MPa) enters a heat supply workshop, and is preheated by a primary nitrogen preheater E303a (100 ℃, 1350 m)3H, 2.3 MPa) into the primary expander EXP1a or EXP1b, and when the temperature is insufficient, the heating is supplemented by the primary steam heaters H101a, H101 b. The outlet gas (50 ℃, 3550 m3/H and 0.65 MPa) of the primary expander EXP1a or EXP1b enters a flue gas heater E304 and a secondary nitrogen preheater E303b for heating, the flue gas heater E304 and the secondary nitrogen preheater E303b can work in parallel or independently, the ratio of the tail gas flow of the flue gas heater E304 and the secondary nitrogen preheater E303b can be adjusted when the flue gas heater E304 and the secondary nitrogen preheater E303b are connected in parallel, the heated tail gas (130 ℃, 4450 m3/H and 0.65 MPa) enters a secondary expander EXP2a or EXP2b, and when the temperature is insufficient, the secondary steam heaters H102a and H102b are used for supplementary heating. Exit tail gas of secondary expander EXP2a and EXP2b (33 ℃, 11500 m)3H, 0.20 MPa) can be directly discharged from an exhaust chimney. The beneficial effects are that: the energy-saving efficiency reaches 50 percent.
Example 3:
oxidation reaction tail gas (35 ℃, 1200 m) of trimellitic anhydride device3H, 2.5 MPa) is firstly sent into a heating workshop and preheated by a primary nitrogen preheater E303a (110 ℃, 1400 m3/h,2.5 MPa) enters a primary expander EXP1a or EXP1b, when the temperature is insufficient, the primary expander is heated by a primary steam heater H101a or H101b in a supplementing way, when the temperature is lower than 95 ℃, the supplementary heating is started, or the steam heater is used for heating tail gas when a heat supply workshop is overhauled. Exit gas (55 ℃, 3600 m) of first expander EXP1a or EXP1b30.7 MPa) enters a flue gas heater E304 and a secondary nitrogen preheater E303b for heating, the flue gas heater E304 and the secondary nitrogen preheater E303b can work in parallel or independently, the ratio of the tail gas flow of the flue gas heater E304 and the tail gas flow of the secondary nitrogen preheater E303b can be adjusted when the flue gas heater E304 and the secondary nitrogen preheater are connected in parallel, and the heated tail gas (150 ℃, 4500 m) is obtained3H, 0.7 MPa) into secondary expander EXP2a or EXP2b, and when the temperature is insufficient, the heating is supplemented by secondary steam heaters H102a, H102 b. Exit tail gas (35 ℃, 12000 m) from secondary expander EXP2a and EXP2b3H, 0.25 MPa) can be directly discharged from an exhaust chimney. The beneficial effects are that: the energy-saving efficiency reaches 45 percent.
Compared with the existing PTA production energy recovery process at home and abroad, the turbine energy recovery process for producing tail gas by the trimellitic anhydride continuous method has the characteristics of capability of recovering medium-pressure low-gas tail gas produced by the trimellitic anhydride continuous method and high energy recovery rate (40-50%). The maximum recycling of tail gas energy and flue gas energy in TMA production is realized, the energy consumption is low, the efficiency is improved, the energy waste is reduced, and the energy-saving guarantee can be provided for the long-term stable operation of the process air compressor.
The utility model discloses a heat transfer and secondary heat transfer have promoted the energy of tail gas, have promoted flow and pressure for the tail gas flow size accords with the requirement of the continuous air feed of one-level expander and second grade expander, thereby reaches the technical requirement of stable recovered energy. The recovered energy is sent into the oxidation reaction device by compressing the raw material air through the primary air compressor and the secondary air compressor, so that the purpose of improving the energy recovery and utilization efficiency is achieved. The method is suitable for recovering the tail gas energy in the production of the trimellitic anhydride by the liquid-phase air continuous oxidation method. The beneficial effects are that:
1) and recovering the energy of the low-temperature low-gas tail gas generated in the TMA production process.
2) The energy of flue nitrogen of an incinerator or a natural gas furnace is utilized.
3) The energy-saving efficiency is 40-50%.
The present invention is not limited to the above embodiments, and based on the technical solutions disclosed in the present invention, those skilled in the art can make some replacements and transformations for some technical features without creative labor according to the disclosed technical contents, and these replacements and transformations are all within the protection scope of the present invention.
Claims (5)
1. A tail gas turbine energy recovery device for continuous production of trimellitic anhydride is characterized in that: the system comprises a primary heat exchange device, a primary turbine, a secondary heat exchange device and a secondary turbine, wherein the primary turbine comprises a primary expansion machine and a primary compressor with a primary expansion machine shaft belt, the secondary turbine comprises a secondary expansion machine and a secondary compressor with a secondary expansion machine shaft belt, the primary compressor and the secondary compressor are used for supplying compressed air to an inlet of an oxidation reaction device, an inlet of the primary heat exchange device is connected with a tail gas pipeline of the oxidation reaction, an outlet of the primary heat exchange device is connected with an inlet of the primary expansion machine, an outlet of the primary expansion machine is connected with an inlet of the secondary heat exchange device, an outlet of the secondary heat exchange device is connected with an inlet of the secondary expansion machine, and an outlet of the secondary expansion machine is communicated with an exhaust.
2. The turbine energy recovery device for the continuous production tail gas of trimellitic anhydride according to claim 1, characterized in that the primary heat exchange device comprises a primary nitrogen preheater and a primary steam heater, and the primary steam heater is arranged between the primary nitrogen preheater and the primary expander.
3. The turbine energy recovery device for the continuous production tail gas of trimellitic anhydride according to claim 2, characterized in that the secondary heat exchange device comprises a secondary nitrogen preheater, a flue gas heater and a secondary steam heater, wherein the secondary nitrogen preheater and the flue gas heater are arranged in parallel, then connected with the secondary steam heater, and then connected to an inlet of a secondary expansion machine.
4. The turbine energy recovery device for the continuous production tail gas of trimellitic anhydride according to claim 3, characterized in that the heat source ends of the primary nitrogen preheater and the secondary nitrogen preheater are connected with flue gas of an oil furnace; the heat source of the flue gas heater is connected with the flue gas of the incinerator.
5. The turbine energy recovery device for the tail gas from the continuous production of the trimellitic anhydride according to any one of claims 1 to 4, characterized in that two groups of primary steam heaters are arranged in parallel with a primary turbine; two groups of secondary steam heaters and two groups of secondary turbines are also arranged in parallel.
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