CN110864577A - Tail end heat energy utilization and emission reduction process for toluene to produce benzoic acid - Google Patents
Tail end heat energy utilization and emission reduction process for toluene to produce benzoic acid Download PDFInfo
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- CN110864577A CN110864577A CN201911178157.2A CN201911178157A CN110864577A CN 110864577 A CN110864577 A CN 110864577A CN 201911178157 A CN201911178157 A CN 201911178157A CN 110864577 A CN110864577 A CN 110864577A
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 title claims abstract description 102
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000005711 Benzoic acid Substances 0.000 title claims abstract description 12
- 235000010233 benzoic acid Nutrition 0.000 title claims abstract description 12
- 238000011946 reduction process Methods 0.000 title claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000003507 refrigerant Substances 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims abstract description 21
- 238000001179 sorption measurement Methods 0.000 claims abstract description 15
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 4
- RZGSPMLEQHFAHD-UHFFFAOYSA-N benzoic acid;toluene Chemical compound CC1=CC=CC=C1.OC(=O)C1=CC=CC=C1 RZGSPMLEQHFAHD-UHFFFAOYSA-N 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 claims 1
- 230000003197 catalytic effect Effects 0.000 abstract description 8
- 230000003647 oxidation Effects 0.000 abstract description 8
- 238000007254 oxidation reaction Methods 0.000 abstract description 8
- 238000010248 power generation Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000002826 coolant Substances 0.000 abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- 239000010865 sewage Substances 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229920000049 Carbon (fiber) Polymers 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 239000004917 carbon fiber Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
- F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a tail end heat energy utilization and emission reduction process of a process for producing benzoic acid by continuous catalytic oxidation of toluene, mixed gas condensed in four steps enters a multi-channel heat exchanger from a first heat medium inlet of the multi-channel heat exchanger, is discharged and then enters an oil-water separator, after toluene and water are separated by the oil-water separator, the mixed gas enters the multichannel heat exchanger from a first refrigerant inlet of the multichannel heat exchanger for heat exchange, the mixed gas discharged from the multichannel heat exchanger enters the heat exchanger, the mixed gas discharged from the heat exchanger enters the worm gear generator set to push the turbine generator to generate electric power, the mixed gas discharged from the worm gear generator set enters the multichannel heat exchanger from a second refrigerant inlet of the multichannel heat exchanger again to cool the first heating medium and the first cooling medium to the designed temperature, and then the refrigerant enters the adsorber from a second refrigerant outlet of the multi-channel heat exchanger, and the exhaust gas meeting the emission standard is obtained after adsorption. The mixed gas power generation is 260kw/hr, three sets of adsorption devices are saved, and the economic benefit generated each year reaches 470 ten thousand.
Description
Technical Field
The invention belongs to the field of energy conservation and environmental protection, and relates to a heat energy utilization technology for producing benzoic acid by continuous catalytic oxidation of toluene, in particular to a tail end heat energy utilization and emission reduction technology for a process for producing benzoic acid by continuous catalytic oxidation of toluene.
Background
The process for producing the benzoic acid by the continuous catalytic oxidation of the toluene comprises four stages of fractional condensation, and the finally obtained mixed gas (containing water vapor and the toluene) has the temperature of 40 ℃ and the pressure of 0.535 MPa. The mixed gas contains a certain amount of toluene, so that the mixed gas has high value, more importantly, the mixed gas cannot be discharged to the atmosphere, the toluene content in the mixed gas must be reduced until the load discharge requirement is met, and the processes of toluene adsorption, water vapor desorption, oil-water separation and the like in the mixed gas are required to be performed by a high-efficiency adsorption carbon fiber felt adsorber, so that the standard discharge is realized finally. Since the mixed gas is not only high in toluene content but also high in temperature, which is disadvantageous in adsorption and low in efficiency, it is necessary to treat this portion of the mixed gas again, and not only the toluene is further separated, but also the calorific value of the mixed gas is further utilized.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a tail end heat energy utilization and emission reduction process of a process for producing benzoic acid by continuous catalytic oxidation of toluene, wherein the tail end heat energy is used for power generation, so that the energy is further saved and the emission is reduced.
The technical scheme adopted by the invention for solving the technical problem is as follows:
a tail end heat energy utilization and emission reduction process method for a process of producing benzoic acid by continuous catalytic oxidation of toluene comprises the steps of enabling mixed gas after four steps of condensation to enter a multi-channel heat exchanger from a first heat medium inlet of the multi-channel heat exchanger, then discharging the mixed gas from a first heat medium outlet and then entering an oil-water separator, enabling the mixed gas after the oil-water separator separates toluene and water to enter the multi-channel heat exchanger from a first refrigerant inlet of the multi-channel heat exchanger for heat exchange, increasing the temperature of the mixed gas, then discharging the mixed gas from a first refrigerant outlet of the multi-channel heat exchanger and then entering the heat exchanger, enabling the heat exchanger to further heat and raise the temperature by using hot water of 90-100 ℃ discharged by the previous step of condensation process, enabling the mixed gas discharged by the heat exchanger to enter a worm gear generator set to push the worm gear generator set to generate electric power, enabling the, and cooling the first heating medium and the first cooling medium to the designed temperature, then entering an adsorber from a second cooling medium outlet of the multichannel heat exchanger, and obtaining exhaust gas meeting the emission standard after adsorption.
And the toluene separated by the oil-water separator enters a toluene storage tank, and the separated water enters a subsequent drainage treatment system.
A tail end heat energy utilization and emission reduction process device for a process for producing benzoic acid by toluene comprises a multi-channel heat exchanger, an oil-water separator, a heat exchanger, a worm gear generator set and an adsorber; a first heat medium inlet of the multi-channel heat exchanger is connected with a mixed gas input pipeline, a first heat medium outlet of the multi-channel heat exchanger is connected with a mixed gas inlet of the oil-water separator through a pipeline, a mixed gas outlet of the oil-water separator is connected with a first refrigerant inlet of the multi-channel heat exchanger through a pipeline, a first refrigerant outlet of the multi-channel heat exchanger is connected with a refrigerant inlet of the heat exchanger through a pipeline, a heat medium inlet of the heat exchanger is connected with a refrigerant outlet pipeline of the second heat exchanger, a heat medium outlet of the heat exchanger is connected with a refrigerant inlet pipeline of the second heat exchanger, a refrigerant outlet of the heat exchanger is connected with a heat source inlet of the worm gear generator set through a pipeline, a heat source outlet of the worm gear generator set is connected with a second refrigerant inlet of the, the outlet of the adsorber is connected with a mixed gas discharge pipeline.
And a toluene outlet of the oil-water separator is connected to a toluene storage tank through a toluene output pipeline, and a condensed water outlet of the oil-water separator is connected to a subsequent drainage treatment system through a condensed water output pipeline.
The invention has the advantages and positive effects that:
1. four sets of adsorption devices are needed in the traditional treatment process, only one set is used in the invention, and three sets of adsorption devices are saved. The economic benefit is up to 470 ten thousand per year.
2. The power generation of the mixed gas is 260kw/hr, the power consumption of the three sets of adsorption devices is saved by 90kw/hr, the power charge per degree is 0.8 yuan per year according to 8000 hours, and 224 ten thousand yuan per year is saved.
3. Three sets of adsorption devices are saved, the amount of water vapor desorbed per hour is 1.8T, the sewage treatment cost per ton is 150 yuan, and the sewage treatment cost is saved by 216 ten thousand yuan per year.
4. The invention reduces the operation of 3 sets of 3 boxes of 8-core activated carbon fiber felt adsorbers, and can save 32.4 ten thousand of expenses each year.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments, which are illustrative only and not limiting, and the scope of the present invention is not limited thereby.
A tail end heat energy utilization and emission reduction process device for a process for producing benzoic acid by continuous catalytic oxidation of toluene comprises a multi-channel heat exchanger 1, an oil-water separator 2, a heat exchanger 3, a worm gear generator set 4 and an absorber 5. The mixed gas after four-step condensation is connected with a first heating medium inlet 6 of the multi-channel heat exchanger 1 through a pipeline, a first heating medium outlet 7 of the multi-channel heat exchanger 1 is connected with a mixed gas inlet of the oil-water separator 2 through a pipeline, a toluene outlet 12 of the oil-water separator 2 is connected with a toluene output pipeline, a mixed gas outlet 14 of the oil-water separator 2 is connected with a first refrigerant inlet 8 of the multi-channel heat exchanger 1 through a pipeline, and a condensed water outlet 13 of the oil-water separator 2 is connected to a subsequent drainage treatment system through a condensed water output pipeline. The first refrigerant outlet 9 of the multichannel heat exchanger 1 is connected with the refrigerant inlet 15 of the heat exchanger 3 through a pipeline, the heat medium inlet 17 of the heat exchanger 3 is connected with a 95 ℃ hot water pipeline, the heat medium outlet 18 of the heat exchanger 3 is connected with a 75 ℃ hot water pipeline, the refrigerant outlet 16 of the heat exchanger 3 is connected with the heat source inlet of the worm gear generator set 4 through a pipeline, the heat source outlet of the worm gear generator set 4 is connected with the second refrigerant inlet 10 of the multichannel heat exchanger 1 through a pipeline, the second refrigerant outlet 11 of the multichannel heat exchanger 1 is connected with the inlet of the adsorber 5 through a pipeline, and the outlet of the adsorber 5 is connected with.
A tail end heat energy utilization and emission reduction process method for a process of producing benzoic acid through continuous catalytic oxidation of toluene comprises the steps of enabling mixed gas (I) subjected to four-step condensation to enter a multi-channel heat exchanger 1 from a first heat medium inlet 6 of the multi-channel heat exchanger 1, further reducing the temperature to obtain mixed gas (Q) at the temperature of 2-3 ℃, discharging the mixed gas (Q) from a first heat medium outlet 7 of the multi-channel heat exchanger 1, enabling the mixed gas (Q) to enter an oil-water separator 2, further removing moisture and toluene in the mixed gas, and obtaining 0.35T/hr mixed gas (S) from a mixed gas outlet of the oil-water separator 2, wherein water vapor is almost little. In order to fully utilize the potential of the mixed gas and facilitate subsequent power generation, the mixed gas (S) enters the multi-channel heat exchanger 1 again from the first refrigerant inlet 8 of the multi-channel heat exchanger 1 for heat exchange, the temperature of the mixed gas is increased to about 10 ℃, and the mixed gas is also a low-temperature source for effectively utilizing the mixed gas from the turbine generator. The heated mixed gas (X) discharged from the first refrigerant outlet 9 of the multi-channel heat exchanger 1 is introduced into the heat exchanger 3, and heated to 70 ℃ by 95 ℃ hot water, and the heat-exchanged 95 ℃ hot water (K) is converted into 75 ℃ hot water (T). At this time, the mixed gas (Y) from the heat exchanger 3 has higher potential, and directly drives a turbine generator to generate 260kw/hr of electric power (U), the temperature and pressure of the discharged mixed gas (V) are respectively reduced to-10 to-8 ℃ and 1.0kgf due to the throttling process, the mixed gas (V) is a good refrigerant, and enters the multi-channel heat exchanger 1 from the second refrigerant inlet 10 of the multi-channel heat exchanger 1 to cool the mixed gas (I) and the mixed gas (S) to the designed temperature. The mixed gas (W) heated to 24 ℃ per se is discharged from the second refrigerant outlet 11 of the multi-channel heat exchanger 1, enters the adsorber 5 and is adsorbed to obtain the exhaust gas (Z) meeting the emission standard.
Four sets of adsorption devices are needed in the traditional treatment process, only one set is used in the invention, and three sets of adsorption devices are saved.
1. The mixed gas power generation is 260kw/hr, the operation power consumption of three sets of adsorption devices is saved by 90kw/hr, the electricity charge per degree is 0.8 yuan according to 8000 hours every year, and the electricity charge is saved every year:
(260+90) x 8000x 0.8-2240000 ten-224 ten thousand yuan
2. The water vapor which is desorbed by three sets of adsorption devices per hour is saved by 1.8T, the sewage treatment cost per ton is 150 yuan, and the sewage treatment cost is saved by 1.8x 8000x 150-2160000-216 ten thousand yuan per year
3. Reduce 3 sets of 3 case 8 core activated carbon fiber felt adsorbers and move, activated carbon fiber felt life is 3 years, and one case has 8 cores, and the activated carbon fiber felt weight of one core is 45kg, and every kg market price is 300 yuan, can save the expense annually:
3x 3x 8x 45Kg x 300 (yuan/Kg)/3 (year) ═ 324000 yuan ═ 32.4 ten thousand yuan
4. The economic benefit is 216+224+32.4 ═ 472.4 ten thousand yuan per year
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various changes and modifications can be made without departing from the inventive concept, and these changes and modifications are all within the scope of the present invention.
Claims (4)
1. A tail end heat energy utilization and emission reduction process method for a process for producing benzoic acid by toluene is characterized by comprising the following steps: the mixed gas after four steps of condensation enters a multichannel heat exchanger from a first heat medium inlet of the multichannel heat exchanger, then is discharged from a first heat medium outlet and enters an oil-water separator, toluene and water are separated by the oil-water separator, then the mixed gas enters the multichannel heat exchanger from a first refrigerant inlet of the multichannel heat exchanger for heat exchange, the temperature of the mixed gas is raised, then the mixed gas is discharged from a first refrigerant outlet of the multichannel heat exchanger and enters the heat exchanger, the heat exchanger utilizes 90-100 ℃ hot water discharged by a previous step of condensation process for heat exchange with the hot water, so that the hot water is further heated and heated, the mixed gas discharged from the heat exchanger enters a worm gear generator set to push the turbine generator set to generate electric power, the mixed gas discharged from the worm gear generator set enters the multichannel heat exchanger from a second refrigerant inlet of the multichannel heat exchanger again, and the first heat medium and the first refrigerant are, and then the refrigerant enters the adsorber from a second refrigerant outlet of the multi-channel heat exchanger, and the exhaust gas meeting the emission standard is obtained after adsorption.
2. The method of claim 1, wherein: and the toluene separated by the oil-water separator enters a toluene storage tank, and the separated water enters a subsequent drainage treatment system.
3. A tail end heat energy utilization and emission reduction process device for a toluene benzoic acid production process is characterized in that: the device comprises a multi-channel heat exchanger, an oil-water separator, a heat exchanger, a worm gear generator set and an adsorber; a first heat medium inlet of the multi-channel heat exchanger is connected with a mixed gas input pipeline, a first heat medium outlet of the multi-channel heat exchanger is connected with a mixed gas inlet of the oil-water separator through a pipeline, a mixed gas outlet of the oil-water separator is connected with a first refrigerant inlet of the multi-channel heat exchanger through a pipeline, a first refrigerant outlet of the multi-channel heat exchanger is connected with a refrigerant inlet of the heat exchanger through a pipeline, a heat medium inlet of the heat exchanger is connected with a refrigerant outlet pipeline of the second heat exchanger, a heat medium outlet of the heat exchanger is connected with a refrigerant inlet pipeline of the second heat exchanger, a refrigerant outlet of the heat exchanger is connected with a heat source inlet of the worm gear generator set through a pipeline, a heat source outlet of the worm gear generator set is connected with a second refrigerant inlet of the, the outlet of the adsorber is connected with a mixed gas discharge pipeline.
4. A process unit according to claim 3, characterized in that: a toluene outlet of the oil-water separator is connected to a toluene storage tank through a toluene output pipeline, and a condensed water outlet of the oil-water separator is connected to a subsequent drainage treatment system through a condensed water output pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911178157.2A CN110864577A (en) | 2019-11-27 | 2019-11-27 | Tail end heat energy utilization and emission reduction process for toluene to produce benzoic acid |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201911178157.2A CN110864577A (en) | 2019-11-27 | 2019-11-27 | Tail end heat energy utilization and emission reduction process for toluene to produce benzoic acid |
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| CN110864577A true CN110864577A (en) | 2020-03-06 |
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| CN201911178157.2A Pending CN110864577A (en) | 2019-11-27 | 2019-11-27 | Tail end heat energy utilization and emission reduction process for toluene to produce benzoic acid |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110922323A (en) * | 2019-11-27 | 2020-03-27 | 天津东大化工集团有限公司 | Thermoelectric coupling efficient energy-saving emission-reducing process for producing benzoic acid by continuous catalytic oxidation of toluene |
| CN112264027A (en) * | 2020-10-27 | 2021-01-26 | 南京工业大学 | Copper-cobalt-cerium composite oxide catalytic combustion catalyst and preparation method and application thereof |
| CN110922323B (en) * | 2019-11-27 | 2024-07-02 | 天津东大化工集团有限公司 | Thermal-electric coupling high-efficiency energy-saving emission-reduction process for producing benzoic acid by continuous catalytic oxidation of toluene |
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| GB803026A (en) * | 1956-03-06 | 1958-10-15 | Dudley Brian Spalding | Plant for a gaseous reaction process |
| JPH06323676A (en) * | 1993-05-13 | 1994-11-25 | Sanyo Electric Co Ltd | Absorptive refrigerator |
| US20150121876A1 (en) * | 2013-11-01 | 2015-05-07 | Panasonic Intellectual Property Management Co., Ltd. | Exhaust heat recovery apparatus, heating system, steam boiler, and deodorization system |
| CN108138588A (en) * | 2015-08-24 | 2018-06-08 | 沙特阿拉伯石油公司 | By the waste-heat power generation in comprehensive aromatic hydrocarbons and naphtha block equipment |
| CN211575954U (en) * | 2019-11-27 | 2020-09-25 | 天津科技大学 | Tail end heat energy utilization and emission reduction process device for toluene production benzoic acid process |
-
2019
- 2019-11-27 CN CN201911178157.2A patent/CN110864577A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB803026A (en) * | 1956-03-06 | 1958-10-15 | Dudley Brian Spalding | Plant for a gaseous reaction process |
| JPH06323676A (en) * | 1993-05-13 | 1994-11-25 | Sanyo Electric Co Ltd | Absorptive refrigerator |
| US20150121876A1 (en) * | 2013-11-01 | 2015-05-07 | Panasonic Intellectual Property Management Co., Ltd. | Exhaust heat recovery apparatus, heating system, steam boiler, and deodorization system |
| CN108138588A (en) * | 2015-08-24 | 2018-06-08 | 沙特阿拉伯石油公司 | By the waste-heat power generation in comprehensive aromatic hydrocarbons and naphtha block equipment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110922323A (en) * | 2019-11-27 | 2020-03-27 | 天津东大化工集团有限公司 | Thermoelectric coupling efficient energy-saving emission-reducing process for producing benzoic acid by continuous catalytic oxidation of toluene |
| CN110922323B (en) * | 2019-11-27 | 2024-07-02 | 天津东大化工集团有限公司 | Thermal-electric coupling high-efficiency energy-saving emission-reduction process for producing benzoic acid by continuous catalytic oxidation of toluene |
| CN112264027A (en) * | 2020-10-27 | 2021-01-26 | 南京工业大学 | Copper-cobalt-cerium composite oxide catalytic combustion catalyst and preparation method and application thereof |
| CN112264027B (en) * | 2020-10-27 | 2021-11-02 | 南京工业大学 | Copper-cobalt-cerium composite oxide catalytic combustion catalyst and preparation method and application thereof |
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