CN210127952U - Turbine expansion compressor and hydrogen peroxide production system comprising same and having energy saving and consumption reduction functions - Google Patents
Turbine expansion compressor and hydrogen peroxide production system comprising same and having energy saving and consumption reduction functions Download PDFInfo
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- CN210127952U CN210127952U CN201920589823.0U CN201920589823U CN210127952U CN 210127952 U CN210127952 U CN 210127952U CN 201920589823 U CN201920589823 U CN 201920589823U CN 210127952 U CN210127952 U CN 210127952U
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- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 230000009467 reduction Effects 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 88
- 230000006835 compression Effects 0.000 claims abstract description 74
- 238000007906 compression Methods 0.000 claims abstract description 74
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 67
- 230000003647 oxidation Effects 0.000 claims abstract description 66
- 238000005516 engineering process Methods 0.000 claims abstract description 7
- 230000006837 decompression Effects 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 39
- 238000001179 sorption measurement Methods 0.000 claims description 28
- 239000007791 liquid phase Substances 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000012224 working solution Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- 229920000049 Carbon (fiber) Polymers 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
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- 238000006243 chemical reaction Methods 0.000 description 3
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 229910000838 Al alloy Inorganic materials 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000013073 enabling process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
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- 229910052742 iron Inorganic materials 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
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- 238000011084 recovery Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The utility model discloses a turbine expansion compressor reaches energy saving and consumption reduction's hydrogen peroxide solution production system including it, turbine expansion compressor include the expansion end and the compression end of connecting through mechanical axis, the input port of compression end be used for with air compressor connects, the compression end is used for further compressing compressed air, the expansion end is used for the oxidation tail gas decompression inflation and the discharge of input, the expansion end turns into mechanical energy with the energy recuperation of expansion oxidation tail gas release and transmits the kinetic energy as the compression end for the compression end through mechanical axis. The utility model discloses combine turbine expansion compressor and air compressor in production technology organically and make per ton hydrogen peroxide solution production air compression part consume the electric energy and fall to 60-85KWh, and the average production per ton 27.5% concentration hydrogen peroxide solution product power consumption reduces about 40KWh on a par, has very practical economic value.
Description
Technical Field
The utility model relates to a hydrogen peroxide solution production and tail gas treatment field especially relate to a turbine expansion compressor and energy saving and consumption reduction's hydrogen peroxide solution production system including it.
Background
The air system flow of the existing hydrogen peroxide production process is as follows, an air compressor is adopted to compress the atmosphere to the pressure of 0.45-0.7MPa (gauge pressure, the pressure below indicates the gauge pressure except the accident), then the atmosphere is cooled to the room temperature, water is separated, the water is filtered and sent to an oxidation reactor for reaction, oxidized tail gas (containing water and working solution solvent components and the like) with the pressure of 0.15-0.25MPa is discharged, the oxidized tail gas is cooled by circulating water to separate liquid, then the liquid is subjected to heat exchange with air at an outlet of an expansion end of an expander, the heat exchange is carried out, the expanded, decompressed and temperature is reduced, the separated liquid is subjected to heat exchange, the gas-liquid separation is carried out, the compressed liquid is subjected to gas-liquid separation, and the working solution solvent. The air compressor in the technology consumes large electric energy, the surplus pressure of the oxidized tail gas is unfavorable for a carbon fiber system, the air compressor end of the expander has to passively recompress and heat the original low-pressure oxidized tail gas for balance (0.08-0.12MPa, the temperature is more than 50 ℃), the use effect of the tail gas adsorption system is further reduced (the adsorption pressure of the tail gas adsorbent is generally not more than 5KPa, the temperature is 20-30 ℃ optimal), the energy of the whole system is surplus, and the electric energy consumed by the compressed part of air produced by each ton of hydrogen peroxide (27.5%) is about 125 KWh.
In the prior art, after a technician cools tail gas by using an expansion end of an expansion machine, a compression end compresses the cooled tail gas to balance energy, so that overtemperature and overpressure of a rear-section carbon fiber tail gas adsorption device are caused, related equipment for pressure reduction and temperature reduction needs to be arranged, the investment is large, the energy consumption is high, the effect is not obvious, the carbon fiber adsorption effect is poor due to the same high temperature, and the aromatic hydrocarbon consumption of the device is high. And the existing hydrogen peroxide device process compressor generally adopts three-stage compression (the maximum can be 0.8MPa, the use pressure is only 0.45-0.5 MPa, and a large amount of design is redundant), needs to be provided with a three-stage cooler, and has low energy utilization efficiency and higher energy consumption.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide an energy utilization rate is high, entire system combines organically, and the system operates steadily, the energy consumption is low, the device construction fixed asset is with small investment and reduce the turbine expansion compressor of the operating energy and material consumption and include its energy saving and consumption reduction's hydrogen peroxide solution production system by a wide margin.
In order to solve the technical problem, the utility model provides a technical scheme as follows:
on one hand, the utility model provides a turbine expansion compressor is used for hydrogen peroxide solution production technology to carry out energy recuperation and utilizes, including expansion end and the compression end through mechanical shaft connection, the input port of compression end be used for with air compressor is connected, the compression end is used for further compressing compressed air, the expansion end is used for decompressing the oxidation tail gas of input and expanding and discharging, the expansion end is converted into mechanical energy with the energy recuperation that releases in the oxidation tail gas expansion process and is transmitted the kinetic energy that the compression end was regarded as the compression end through the mechanical shaft;
furthermore, the expansion end is a turbine expander, and an expander impeller connected with one end of the mechanical shaft is arranged in the turbine expander; the compression end is a centrifugal supercharger, and a supercharger impeller connected with the other end of the mechanical shaft is arranged in the centrifugal supercharger; the expander impeller, the mechanical shaft and the supercharger impeller rotate coaxially; the expander impeller rotates by energy generated by the expansion of the oxidized exhaust gas, drives the mechanical shaft to rotate and transmits the energy to the supercharger impeller, and air compression is performed by the rotation of the supercharger impeller.
Furthermore, shaft seals are arranged at the joints of the mechanical shaft and the expansion end and the compression end.
Further, the turbo expander further comprises a volute used for installing the expander impeller, and an adjustable nozzle used for adjusting the air flow entering the expansion impeller is arranged in the volute.
Further, centrifugal booster compressor is still including being used for the installation the pressure boost spiral case of booster compressor impeller, still be equipped with inlet chamber, no leaf diffuser and blast pipe in the pressure boost spiral case, the mechanical power drive booster compressor impeller that the expander impeller sent is rotatory and enter the further speed reduction pressure boost of no leaf diffuser, through blast pipe exhaust compressed air.
Furthermore, the compression ratio of the supercharger impeller is 1.4-1.7.
On the other hand, the hydrogen peroxide production system with energy conservation and consumption reduction is provided, and comprises the turbine expansion compressor, an air compressor and an oxidation reactor; an input port of a compression end of the turbine expansion compressor is connected with an air compressor and used for further compressing the compressed air, and an output port of the compression end is connected with an input port of the oxidation reactor; the exhaust port of the oxidation reactor is connected with the input port of the expansion end of the turbine expansion compressor, the oxidation tail gas exhausted by the oxidation reactor enters the expansion end, the expansion end is used for decompressing, expanding and exhausting the input oxidation tail gas, and the expansion end recovers and converts the energy released by the expansion oxidation tail gas into mechanical energy and transmits the mechanical energy to the compression end through a mechanical shaft to serve as the kinetic energy of the compression end.
And the adsorption device is used for adsorbing working liquid in the expanded oxidized tail gas output by the expansion end so that the oxidized tail gas reaches the emission standard.
Further, a first gas-liquid separator is connected between the output port and the expansion end of the oxidation reactor, and the first gas-liquid separator is used for separating a liquid phase in the oxidation tail gas and inputting the oxidation tail gas into the expansion end.
Further, a second gas-liquid separator is connected between the expansion end and the adsorption device and is used for separating a liquid phase in the expanded oxidation tail gas output by the expansion end and inputting the liquid phase into the adsorption device.
Furthermore, a connecting pipeline between the second gas-liquid separator and the adsorption device is a straight-through pipe provided with a first valve, and the straight-through pipe is connected with a heat exchanger connected with the first valve in parallel to form a main path and a bypass of the heat exchanger.
Furthermore, a second valve positioned between the first valve and the adsorption device is also arranged on the straight-through pipe, and the straight-through pipe is connected with a temperature regulator connected with the second valve in parallel.
Further, the heat exchanger is connected in parallel with a pipeline between the compression end and the oxidation reactor and is used for adjusting the temperature of the expanded oxidation tail gas by utilizing the heat of the compressed air.
Further, a compressed gas buffer tank is connected between the compression end and the air compressor.
Further, an air filter is connected between the compression end and the oxidation reactor.
Furthermore, a through pipe provided with a valve is directly connected between the input port and the output port of the compression end.
Furthermore, a through pipe provided with a valve is directly connected between the input port and the output port of the expansion end.
After adopting such design, the utility model discloses following advantage has at least:
1) the utility model discloses a production system obtains compressed air through compressing the air compressor machine for the atmosphere to assigned pressure, and compressed air obtains the process air through the required pressure of turbo expansion compressor's compression end pressure boost to entering oxidation reactor and filtering after, the process air gets into the oxidation tail gas that the discharge obtained certain pressure behind oxidation reactor and the oxidizing liquid reaction, oxidation tail gas gets into the expansion end inflation decompression cooling back of turbo expansion compressor through pressure control after the liquid drop that the vapour and liquid separator went to locate secretly through pressure control, and after the working solution solvent component back part or whole in retrieving oxidation tail gas through the vapour and liquid separator was through the air heat transfer with expander compression end export, and part or whole are after air cooling or water cooling plant temperature regulation again, get into tail gas adsorption equipment and adsorb back emission up to standard.
2) The utility model discloses select for use the high and economic turbine expansion compressor model of energy recuperation and the low air compressor of energy consumption, combine with turbine expansion compressor and air compressor in production technology organically and make per ton hydrogen peroxide solution (27.5%) produce the air compression part and consume the electric energy and reduce to 60-85KWh, per ton product power consumption reduces about 40 degrees, to the one set of 10 ten thousand tons/year (27.5%) output the apparatus for producing of hydrogen peroxide solution, can save energy more than 4,000,000KWh every year, have very practical economic value, the mechanical energy through expansion end release acts on the further compressed air of compression end, can effectual reduction in production cost.
Drawings
The foregoing is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clear, the present invention will be further described in detail with reference to the accompanying drawings and the detailed description.
FIG. 1 is a schematic view of the connection structure of the energy-saving and consumption-reducing hydrogen peroxide production system of the present invention;
fig. 2 is a schematic structural view of the turbo expansion compressor of the present invention.
Detailed Description
Exemplary embodiments of the present invention will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the invention are shown in the drawings, it should be understood that the invention can be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
The utility model provides an embodiment of turboexpansion compressor, as shown in fig. 1, fig. 2 for hydrogen peroxide solution production technology carries out energy recuperation and utilizes, include expansion end 10a and compression end 10b connected through mechanical axis 100, compression end 10 b's input port is connected with air compressor 1, compression end 10b is used for further compressing compressed air, expansion end 10a is used for the oxidation tail gas decompression expansion of input and discharges, and expansion end 10a converts the energy recuperation that releases into mechanical energy and transmits the kinetic energy as the compression end for compression end 10b through the mechanical axis in with oxidation tail gas inflation process.
The utility model discloses when using, after carrying out preliminary compression to the air through air compressor, input turbine expansion compressor's compression end further compression, the mechanical energy that releases when expanding oxidation tail gas through turbine expansion compressor's inflation end transmits to the compression end, further compressed air as the kinetic energy of compression end, the utility model discloses through adopting the turbine expansion compressor model that energy recuperation is high and economic and low pressure centrifugal air compressor that energy consumption is low, combine both organically in the production technology and make per ton hydrogen peroxide solution (27.5%) production air compression part consume the electric energy reduce to 60-85KWh, per ton product power consumption reduces about 40 degrees, to a set of hydrogen peroxide solution production device of 10 ten thousand tons/year (27.5%) output, can save energy more than 4,000,000KWh every year, have very practical economic value, namely the mechanical energy through inflation end release acts on the compression end and further compresses air, the production cost can be effectively reduced.
Further, the expansion end 10a is a turboexpander, and an expander impeller 101 connected to one end of the mechanical shaft 100 is provided in the turboexpander; the compression end 10b is a centrifugal supercharger, and a supercharger impeller 102 connected with the other end of the mechanical shaft 100 is arranged in the centrifugal supercharger; the expander impeller 101, the machine shaft 100, and the supercharger impeller 102 rotate coaxially; the expander impeller 101 rotates by energy generated by the expansion of the oxidized exhaust gas, drives the mechanical shaft 100 to rotate, transmits the energy to the supercharger impeller 102, and compresses air by the rotation of the supercharger impeller 102.
Further, the joints of the mechanical shaft 100 and the expansion end 10a and the compression end 10b are provided with shaft seals.
Further, the turbo expander further comprises a volute for mounting the expander impeller 101, and an adjustable nozzle for adjusting the flow rate of air entering the expander impeller is arranged in the volute.
Further, the centrifugal supercharger also comprises a supercharging volute used for mounting the supercharger impeller 102, an air inlet chamber, a vaneless diffuser and an exhaust pipe are further arranged in the supercharging volute, the supercharger impeller is driven to rotate by mechanical power emitted by the expander impeller 101 and enters the vaneless diffuser for further speed reduction and supercharging, and compressed air is exhausted through the exhaust pipe.
The compression ratio of the supercharger impeller is 1.4-1.7, generally about 1.6 by adjusting the angle and the number of the fan blades of the supercharger impeller.
In the turbo expander: the oxidized tail gas enters the turbine volute from the inlet pipe, enters the working wheel to do work through the rotating nozzle, and is discharged through the diffusion chamber and the exhaust pipe. The turbo expander continuously converts kinetic energy into mechanical energy by expanding a high-pressure gas flow from the front of the unit into a low-pressure gas flow. The high-speed airflow rotates the impeller, and then mechanical energy is transferred to the compressor through a rotating shaft supported by the bearing, so that the energy of the compressor is consumed. The material of the flow passage part of the expander is stainless steel or aluminum alloy. The volute is of a stainless steel casting structure, is fixed on the machine body and is connected with the base through the machine body, and an adjustable nozzle and an expander impeller are arranged in the volute.
In the centrifugal supercharger: the booster consists of air inlet chamber, impeller, vaneless diffuser and volute, the impeller and the impeller are set on the same shaft, and the rotation speed of the two is the same, the mechanical power from the impeller drives the rotation of the impeller, and the gas is accelerated and pressurized after entering the impeller, further decelerated and pressurized after entering the vaneless diffuser, and finally collected to the volute and exhausted outside the machine. The flow-through part of the supercharger is made of carbon steel or aluminum alloy.
On the other hand, the hydrogen peroxide production system with energy conservation and consumption reduction is provided, and comprises the turbine expansion compressor 10, an air compressor 1 and an oxidation reactor 6; the input port of the compression end 10b of the turboexpansion compressor 10 is connected with the air compressor 1 and used for further compressing the compressed air, and the output port of the compression end 10b is connected with the input port of the oxidation reactor 6; the exhaust port of the oxidation reactor 6 is connected with the input port of the expansion end 10a of the turbine expansion compressor 10, the oxidation tail gas exhausted from the oxidation reactor 6 enters the expansion end 10a, the expansion end 10a is used for decompressing, expanding and exhausting the input oxidation tail gas, and the expansion end 10a recovers and converts the energy released by the expansion oxidation tail gas into mechanical energy and transmits the mechanical energy to the compression end 10b through a mechanical shaft to serve as the kinetic energy of the compression end 10 b.
In order to make the oxidized tail gas discharged from the expansion end reach the emission standard, the exhaust gas treatment device further comprises an adsorption device 15, and the adsorption device 15 is used for adsorbing the working fluid in the expanded oxidized tail gas output from the expansion end 10a so as to make the oxidized tail gas reach the emission standard.
In order to improve the adsorption effect, a second gas-liquid separator 12 is connected between the expansion end 10a and the adsorption device 15, and is used for separating the liquid phase in the expanded oxidized tail gas output by the expansion end 10a and inputting the separated liquid phase into the adsorption device 15.
In order to better regulate the temperature of the expanded oxidation tail gas, the connecting pipeline between the second gas-liquid separator 12 and the adsorption device 15 is a straight-through pipe provided with a first valve, and the straight-through pipe is connected with a heat exchanger 13 connected with the first valve in parallel, so that a main path and a bypass of the heat exchanger are formed, and the expanded oxidation tail gas can not pass through, partially pass through or completely pass through the heat exchanger to carry out certain heat exchange.
For better energy utilization, a heat exchanger 13 is also connected in parallel with the pipeline between the compression end 10b and the oxidation reactor 6 for adjusting the temperature of the expanded oxidation tail gas by using the heat of the compressed air, i.e. heat exchange is performed by using the heat of the high compressed air and the low temperature of the expanded oxidation tail gas, thereby further utilizing the recovered energy.
In order to adjust the temperature of the expanded tail gas more conveniently, a second valve is arranged between the first valve and the adsorption device 15 on the straight-through pipe, and the straight-through pipe is connected with a temperature regulator 14 connected with the second valve in parallel.
In order to separate the liquid phase carried out by the oxidation tail gas, a first gas-liquid separator 8 is connected between the output port of the oxidation reactor 6 and the expansion end 10a, and the first gas-liquid separator 8 is used for separating the liquid phase in the oxidation tail gas and inputting the oxidation tail gas into the expansion end 10 a.
The first gas-liquid separator and the second gas-liquid separator can recycle the separated liquid phase.
For convenience, a compressed gas buffer tank 2 is connected between the compression end 10b and the air compressor 1.
An air filter 4 is connected between the compression end 10b and the oxidation reactor 6 in order to remove impurities such as iron filings and dust in the compressed air.
Furthermore, a through pipe with a valve is directly connected between the input port and the output port of the compression end 10 b.
Furthermore, a through pipe with a valve, namely a temperature adjusting pipeline 17, is directly connected between the input port and the output port of the expansion end 10 a.
In the above embodiments, the air compressor is a centrifugal air compressor or a roots blower, and may be any type of compressor capable of compressing atmospheric air to 0.20 to 0.45 MPa.
When the utility model is used, the air compressor 1 extracts the air 1a in the atmosphere and compresses the air to 0.20-0.45 Mpa; storing the compressed air to the pressure of a buffer storage stable air compressor to obtain compressed air 3 a; inputting the compressed air 3a into a compression end 10b of a turbine expansion compressor 10, and compressing the compressed air 3a to the compressed air 3b with the use pressure of 0.25-0.55 MPa; the expansion end 10a converts the energy of the pressure and the temperature recovered by expanding the oxidized tail gas 9 to the expanded tail gas 11 into the kinetic energy of the compression end 10 b; the air filter 4 filters the compressed air 3b to obtain process air 5; inputting process air into an oxidation reactor 6, which is a main device for carrying out oxidation reaction in hydrogen peroxide production and only needs to meet production requirements; the process air 5 reacts with the oxidizing liquid in the oxidation reactor 6 and then is discharged to obtain oxidized tail gas 7, the oxidized tail gas 7 is separated into a possibly entrained liquid phase in a first gas-liquid separator 8 to obtain oxidized tail gas 9, the oxidized tail gas 9 enters an expansion end 10a of a turbine expansion compressor 10, the temperature and pressure are reduced to 0-25 ℃ and 1-50KPa, low-temperature expanded oxidized tail gas 11 is obtained, the low-temperature expanded oxidized tail gas 11 passes through an expanded tail gas-liquid separator to recover the liquid phase (working fluid components and water), and the expansion end 10a is provided with a temperature and pressure regulating pipeline 17; liquid phases 18 and 19 separated by the first gas-liquid separator 8 and the second gas-liquid separator 12 are subjected to oil-water separation and then are recycled; after the low-temperature expanded tail gas 11 is subjected to liquid phase recovery through the second gas-liquid separator 12, part or all of the low-temperature expanded tail gas enters a heat exchanger 13 to exchange heat or part or all of the low-temperature expanded tail gas passes through a bypass without exchanging heat according to process requirements, and part or all of the low-temperature expanded tail gas passes through a temperature regulator 14 to regulate the temperature or passes through the bypass; waste gas 16 which reaches the national waste gas emission standard after entering an adsorption device 15 to adsorb and recover more than 90 percent of working solution components is directly discharged into the atmosphere; the recovered liquid phase 20 is recycled; the utility model has no special requirements for the structure and form of the second gas-liquid separator 12, the heat exchanger 13 and the temperature regulator 14 and the cooling medium thereof, as long as the heat exchange and separation effects can be achieved; the adsorption equipment is the mature product in market, the utility model discloses do not have special requirement to it, only need satisfy the adsorption effect that the national standard required can.
Specific examples may be: the method comprises the steps of compressing air 1a through an air compressor 1 to enable the air to be compressed to 0.25MPa, conveying the air to a buffer tank 2 to stabilize the pressure to obtain compressed air 3a, compressing the compressed air 3a to 0.35MPa through a compression end of a turbine expansion compressor 10 to obtain compressed air 3b, filtering the compressed air through a filter 4, enabling process air 5 to enter an oxidation reactor 6 to react, control the top pressure to be 0.22MPa, discharging oxidation tail gas 7, separating and recovering a liquid phase 18 through a first gas-liquid separator 8, controlling the pressure of a gas phase part 9 to be 0.21MPa, enabling the process air 5 to enter an expansion end 10a of the turbine expansion compressor 10 to expand at 50 ℃, reducing the pressure and reducing the temperature to 3KPa and 5 ℃ through a temperature adjusting mechanism 17 to obtain low-temperature expansion tail gas 11, separating and recovering the liquid phase 19 in an expansion tail gas-liquid separator 12, enabling the gas phase to enter an adsorption device to recover an organic phase by, the content of aromatic hydrocarbon in tail gas is less than 60mg/m3And then discharged to the atmosphere.
The utility model discloses a production system obtains compressed air through compressing the air compressor machine for the atmosphere to assigned pressure, and compressed air obtains the process air through the required pressure of turbo expansion compressor's compression end pressure boost to entering oxidation reactor and filtering after, the process air gets into the oxidation tail gas that the discharge obtained certain pressure behind oxidation reactor and the oxidizing liquid reaction, oxidation tail gas gets into the expansion end inflation decompression cooling back of turbo expansion compressor through pressure control after the liquid drop that the vapour and liquid separator went to locate secretly through pressure control, and after the working solution solvent component back part or whole in retrieving oxidation tail gas through the vapour and liquid separator was through the air heat transfer with expander compression end export, and part or whole are after air cooling or water cooling plant temperature regulation again, get into tail gas adsorption equipment and adsorb back emission up to standard.
The utility model discloses can be applied to hydrogen peroxide solution trade air system and the similar waste energy recycle energy saving and consumption reduction's of chemical industry occasion, have simple process, safe and reliable, current device can reform transform the advantage that utilizes, the small investment, the return is high and the benefit is showing.
The above description is only for the preferred embodiment of the present invention, and not intended to limit the present invention in any way, and those skilled in the art can make various modifications, equivalent changes and modifications using the above-described technical content, all of which fall within the scope of the present invention.
Claims (10)
1. The utility model provides a turbo expansion compressor, its characterized in that for hydrogen peroxide solution production technology carries out energy recuperation and utilizes, includes expansion end and compression end through mechanical axis connection, the input port of compression end is used for being connected with air compressor, the compression end is used for further compressing compressed air, the expansion end is used for the oxidation tail gas decompression expansion and the discharge of input, the expansion end converts the energy recuperation that releases in with oxidation tail gas expansion process into mechanical energy and transmits the kinetic energy as the compression end for the compression end through the mechanical axis.
2. The turboexpansion compressor of claim 1, wherein said expansion end is a turboexpander having an expander impeller therein connected to one end of said machine shaft;
the compression end is a centrifugal supercharger, and a supercharger impeller connected with the other end of the mechanical shaft is arranged in the centrifugal supercharger;
the expander impeller, the mechanical shaft and the supercharger impeller rotate coaxially; the expander impeller rotates by energy generated by the expansion of the oxidized exhaust gas, drives the mechanical shaft to rotate and transmits the energy to the supercharger impeller, and air compression is performed by the rotation of the supercharger impeller.
3. The turbo-expansion compressor of claim 2, further comprising a volute housing the expander wheel, the volute housing further having an adjustable nozzle for adjusting the flow of air into the expansion wheel;
and/or the centrifugal supercharger also comprises a supercharging volute used for mounting the supercharger impeller, an air inlet chamber, a vaneless diffuser and an exhaust pipe are also arranged in the supercharging volute, the supercharger impeller is driven to rotate by mechanical work sent by the expander impeller and enters the vaneless diffuser for further speed reduction and supercharging, and compressed air is exhausted through the exhaust pipe;
and/or the compression ratio of the supercharger impeller is 1.4-1.7.
4. The turboexpansion compressor of claim 1, wherein the mechanical shaft is sealed at the connection between the mechanical shaft and the expansion end and the compression end.
5. An energy-saving and consumption-reducing hydrogen peroxide production system is characterized by comprising the turbo expansion compressor as claimed in any one of claims 1 to 4, an air compressor and an oxidation reactor;
an input port of a compression end of the turbine expansion compressor is connected with an air compressor and used for further compressing the compressed air, and an output port of the compression end is connected with an input port of the oxidation reactor;
the exhaust port of the oxidation reactor is connected with the input port of the expansion end of the turbine expansion compressor, the oxidation tail gas exhausted by the oxidation reactor enters the expansion end, the expansion end is used for decompressing, expanding and exhausting the input oxidation tail gas, and the expansion end recovers and converts the energy released by the expansion oxidation tail gas into mechanical energy and transmits the mechanical energy to the compression end through a mechanical shaft to serve as the kinetic energy of the compression end.
6. An energy-saving and consumption-reducing hydrogen peroxide production system according to claim 5, further comprising an adsorption device, wherein the adsorption device is used for adsorbing working liquid in the expanded oxidized tail gas output by the expansion end so that the oxidized tail gas reaches the emission standard.
7. The energy-saving and consumption-reducing hydrogen peroxide production system according to claim 6, wherein a first gas-liquid separator is further connected between the output port and the expansion end of the oxidation reactor, and the first gas-liquid separator is used for separating a liquid phase in the oxidized tail gas and inputting the oxidized tail gas into the expansion end.
8. The energy-saving and consumption-reducing hydrogen peroxide production system according to claim 7, wherein a second gas-liquid separator is connected between the expansion end and the adsorption device, and is used for separating a liquid phase in the expanded oxidized tail gas output from the expansion end and inputting the liquid phase into the adsorption device.
9. An energy-saving and consumption-reducing hydrogen peroxide production system as claimed in claim 8, wherein the connecting pipeline between the second gas-liquid separator and the adsorption device is a straight-through pipe provided with a first valve and a second valve;
the straight-through pipe is connected with a heat exchanger connected with the first valve in parallel to form a main path and a bypass of the heat exchanger; the straight-through pipe is also provided with a second valve positioned between the first valve and the adsorption device, and the straight-through pipe is connected with a temperature regulator connected with the second valve in parallel
The heat exchanger is also connected in parallel with a pipeline between the compression end and the oxidation reactor and is used for adjusting the temperature of the expanded oxidation tail gas by utilizing the heat of the compressed air.
10. An energy-saving and consumption-reducing hydrogen peroxide production system according to any one of claims 5 to 9, wherein a compressed gas buffer tank is further connected between the compression end and the air compressor;
and/or an air filter is connected between the compression end and the oxidation reactor;
and/or a through pipe provided with a valve is directly connected between the input port and the output port of the compression end;
and/or a through pipe provided with a valve is directly connected between the input port and the output port of the expansion end.
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| CN201920589823.0U CN210127952U (en) | 2019-04-26 | 2019-04-26 | Turbine expansion compressor and hydrogen peroxide production system comprising same and having energy saving and consumption reduction functions |
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| CN201920589823.0U CN210127952U (en) | 2019-04-26 | 2019-04-26 | Turbine expansion compressor and hydrogen peroxide production system comprising same and having energy saving and consumption reduction functions |
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