CN220026955U - Fixed bed furfural hydrogenation reaction system of driving fast - Google Patents
Fixed bed furfural hydrogenation reaction system of driving fast Download PDFInfo
- Publication number
- CN220026955U CN220026955U CN202321127775.6U CN202321127775U CN220026955U CN 220026955 U CN220026955 U CN 220026955U CN 202321127775 U CN202321127775 U CN 202321127775U CN 220026955 U CN220026955 U CN 220026955U
- Authority
- CN
- China
- Prior art keywords
- fixed bed
- bed reactor
- hydrogen
- furfural
- shell side
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- 238000010438 heat treatment Methods 0.000 claims abstract description 34
- 239000002994 raw material Substances 0.000 claims abstract description 27
- 238000003860 storage Methods 0.000 claims abstract description 19
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 239000001257 hydrogen Substances 0.000 claims description 85
- 229910052739 hydrogen Inorganic materials 0.000 claims description 85
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 83
- 239000007789 gas Substances 0.000 claims description 47
- 239000012071 phase Substances 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 13
- 239000006200 vaporizer Substances 0.000 claims description 8
- 230000004913 activation Effects 0.000 abstract description 5
- 230000001105 regulatory effect Effects 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000004904 shortening Methods 0.000 abstract description 4
- 239000003921 oil Substances 0.000 description 43
- 230000009467 reduction Effects 0.000 description 22
- 239000000047 product Substances 0.000 description 19
- XPFVYQJUAUNWIW-UHFFFAOYSA-N furfuryl alcohol Chemical compound OCC1=CC=CO1 XPFVYQJUAUNWIW-UHFFFAOYSA-N 0.000 description 15
- 238000000034 method Methods 0.000 description 14
- 230000008569 process Effects 0.000 description 12
- VQKFNUFAXTZWDK-UHFFFAOYSA-N 2-Methylfuran Chemical compound CC1=CC=CO1 VQKFNUFAXTZWDK-UHFFFAOYSA-N 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- JWUJQDFVADABEY-UHFFFAOYSA-N 2-methyltetrahydrofuran Chemical compound CC1CCCO1 JWUJQDFVADABEY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical group 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a fast starting system for a fixed bed furfural hydrogenation reaction; the device comprises a raw material pretreatment system, wherein a gas phase outlet of the raw material pretreatment system is connected with a tube side of a fixed bed reactor, a catalyst layer is filled in the tube side of the fixed bed reactor, a shell side outlet of the fixed bed reactor is connected with a heat conduction oil storage tank through a heat conduction oil heat exchange unit, and a heat conduction oil pump of the heat conduction oil storage tank is connected with a shell side inlet of the fixed bed reactor; the heat transfer oil heat exchange unit comprises a heating part and a cooling part which are arranged in parallel. The heat transfer oil heat exchange unit is arranged at the shell side outlet of the fixed bed reactor, so that the temperature in the fixed bed reactor can be regulated and controlled, the temperature control speed is improved, the temperature is stably increased and reduced, the temperature fluctuation of the fixed bed reactor is reduced, the quick and stable starting of the fixed bed furfural hydrogenation reaction is ensured, the activation temperature of the catalyst can be reached relatively quickly, and the production of unqualified products is reduced on the basis of shortening the starting time.
Description
Technical Field
The utility model relates to a fast starting system for a fixed bed furfural hydrogenation reaction.
Background
The furfuryl alcohol, 2-methyl furan and other products produced by hydrogenating furfural are important fine chemical intermediate products, and the hydrogenation process can be divided into gas-phase hydrogenation process and liquid-phase hydrogenation process according to different raw material phases, and the gas-phase hydrogenation process is popular due to the advantages of mild reaction conditions, less product impurities, high yield and the like. The gas phase hydrogenation process generally adopts a fixed bed hydrogenation reactor, the catalyst is filled in a fixed bed tube array, and the operation of reducing and heating the catalyst is also needed before the catalyst is used.
The traditional catalyst reduction heating operation mainly adopts an independent system to heat gas, the heated gas enters a tube side of a fixed bed to heat, the mode causes slow temperature rise speed of catalyst reduction, the temperature fluctuation of the fixed bed reactor is large, meanwhile, the activation temperature of the catalyst in the fixed bed reactor is low, a large amount of unqualified products can appear in the early-stage driving production process due to the low temperature, and the defect of raw material waste exists.
Disclosure of Invention
The utility model aims to provide a fast starting system for a fixed bed furfural hydrogenation reaction, which aims to solve the problems in the background technology.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
the quick starting system for the fixed bed furfural hydrogenation reaction comprises a raw material pretreatment system, wherein a gas phase outlet of the raw material pretreatment system is connected with a tube side of a fixed bed reactor, a catalyst layer is filled in the tube side of the fixed bed reactor, a shell side outlet of the fixed bed reactor is connected with a heat conduction oil storage tank through a heat conduction oil heat exchange unit, and a heat conduction oil pump of the heat conduction oil storage tank is connected with a shell side inlet of the fixed bed reactor;
the heat conduction oil heat exchange unit comprises a heating part and a cooling part which are arranged in parallel.
Preferably, the heating part comprises a heat conduction oil heater with a first valve at an inlet.
Preferably, the cooling part comprises a steam drum with a second valve at the inlet for generating steam.
The utility model also comprises a tube side outlet of the fixed bed reactor connected with the tube side of the gas-gas heat exchanger, wherein the tube side outlet of the gas-gas heat exchanger is connected with the shell side inlet of the hydrogen preheater, the shell side gas phase outlet of the hydrogen preheater is connected with the shell side inlet of the cooler, and the shell side gas phase outlet of the cooler is connected with the hydrogen buffer tank; the shell side liquid phase outlet of the hydrogen preheater is connected with the product tank.
Preferably, the shell side liquid phase outlet of the cooler is connected with the water tank.
Preferably, the outlet of the hydrogen buffer tank is connected with the first tee joint through the tube side of the hydrogen preheater and the shell side of the gas-gas heat exchanger, the second end of the first tee joint is connected with the second tee joint through a third valve, and the third end of the first tee joint is connected with the vaporizer in the raw material pretreatment system through a fourth valve; the second tee joint is arranged between a gas phase outlet of the raw material pretreatment system and a tube side of the fixed bed reactor, and a fifth valve is arranged between the raw material pretreatment system and the second tee joint.
Preferably, a hydrogen on-line analyzer and a hydrogen compressor are arranged between the shell side gas phase outlet of the cooler and the hydrogen buffer tank, and the inlet of the hydrogen buffer tank is also connected with a hydrogen pipeline.
Preferably, a sixth valve is arranged between the shell side liquid phase outlet of the hydrogen preheater and the product tank for connection; a seventh valve is arranged between the shell side liquid phase outlet of the cooler and the water tank.
Preferably, a vaporizer inlet in the raw material pretreatment system is connected with a furfural storage tank.
The beneficial effects of the utility model are as follows:
1. the method is suitable for producing furfuryl alcohol or 2-methyl furan and other serial products by hydrogenation of the fixed bed furfural, and is especially suitable for producing furfuryl alcohol, 2-methyl furan and 2-methyl tetrahydrofuran products by hydrogenation of the fixed bed furfural by taking copper element as a main component of the catalyst.
2. According to the utility model, the heat transfer oil heat exchange unit is arranged at the shell side outlet of the fixed bed reactor, so that the temperature in the fixed bed reactor can be regulated and controlled, the fixed bed reactor is operated in a catalyst reduction heating stage and a normal starting operation stage, when the fixed bed reactor is in the catalyst reduction heating stage, the temperature can be regulated and controlled by the heating part and the cooling part according to the initial stage of the heating stage, the main stage of the heating stage, the later stage of the heating stage and the final stage of the heating stage, and when the fixed bed reactor is in the normal starting operation stage, the temperature is regulated and controlled by the cooling part, so that the temperature control speed is improved, the temperature fluctuation of the fixed bed reactor is reduced, the quick and stable starting of the fixed bed hydrogenation reaction is ensured, the catalyst activation temperature can be reached relatively quickly, and the generation of undesirable products is reduced on the basis of shortening the starting time.
3. According to the utility model, the plurality of heat exchange devices are arranged at the tube side outlet of the fixed bed reactor, the characteristic of sharing in the catalyst reduction heating stage and the normal starting operation stage can be realized through the arrangement of the heat exchange devices, and the independent water tank is arranged on the basis for collecting the reduced water generated in the catalyst reduction heating stage, so that the water yield and the water yield of the reduced water are monitored, and the judgment of the period of the catalyst reduction heating stage is facilitated.
4. The full-load operation from the catalyst reduction heating-up stage to the normal driving operation stage takes about 5 days, and the time can be shortened to be less than 72 hours by using the utility model.
5. The utility model uses an independent hydrogen circulation system, and can meet the requirements of a catalyst reduction heating stage and a normal starting operation stage by utilizing the circulation of hydrogen, and simultaneously reduce the resistance of pipeline equipment in the starting stage so as to achieve the purpose of reducing the power consumption of the hydrogen compressor.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
In the figure: 1. a fixed bed reactor; 2. a first valve; 3. a second valve; 4. a heat conducting oil heater; 5. a steam drum; 6. a heat transfer oil storage tank; 7. a thermally conductive oil pump; 8. a gas-gas heat exchanger; 9. a hydrogen preheater; 10. a cooler; 11. a hydrogen on-line analyzer; 12. a hydrogen compressor; 13. a hydrogen line; 14. a hydrogen buffer tank; 15. a seventh valve; 16. a water tank; 17. a sixth valve; 18. a product tank; 19. a fourth valve; 20. a third valve; 21. a raw material pretreatment system; 22. a furfural storage tank; 23. a first tee; 24. a second tee; 25. and a fifth valve.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
Referring to fig. 1, a fast starting system for a fixed bed furfural hydrogenation reaction includes a raw material pretreatment system 21, a gas phase outlet of the raw material pretreatment system 21 is connected with a tube side of a fixed bed reactor 1, and a catalyst layer is filled in the tube side of the fixed bed reactor 1, and is characterized in that: the shell side outlet of the fixed bed reactor 1 is connected with a heat conducting oil storage tank 6 through a heat conducting oil heat exchange unit, and a heat conducting oil pump 7 of the heat conducting oil storage tank 6 is connected with the shell side inlet of the fixed bed reactor 1; the heat conduction oil heat exchange unit comprises a heating part and a cooling part which are arranged in parallel. The method is suitable for series products such as furfuryl alcohol or 2-methyl furan and the like produced by the hydrogenation of the fixed bed furfural, and is particularly suitable for the production of furfuryl alcohol, 2-methyl furan and 2-methyl tetrahydrofuran products produced by the hydrogenation of the fixed bed furfural by taking copper element as a main component of the catalyst; according to the utility model, the heat transfer oil heat exchange unit is arranged to regulate and control the temperature of the tube side of the fixed bed reactor 1, so that the temperature control speed is improved, the temperature is stably raised and lowered, the temperature fluctuation of the fixed bed reactor is reduced, the quick and stable starting of the fixed bed furfural hydrogenation reaction is ensured, the activation temperature of the catalyst can be reached relatively quickly, and the generation of undesirable products is reduced on the basis of shortening the starting time. In a specific use process, the temperature requirements of a catalyst reduction heating stage and a normal start-up operation stage are utilized to heat, cool and preserve heat of a tube side of the fixed bed reactor 1; wherein the heating part comprises a heat conducting oil heater 4 with a first valve 2 at the inlet. The heat conduction oil heater 4 can be in a heat exchange or energy heating mode, and the energy heating can be realized in a conventional electric heating mode and the like; the cooling part comprises a steam drum 5 with a second valve 3 at the inlet for generating steam. Steam is generated by heat exchange with the steam drum 5, so that the purpose of cooling heat conduction oil is achieved, and the cooling or heat preservation of the tube side of the fixed bed reactor 1 is realized by the circulation of the heat conduction oil.
Further, the utility model also comprises a tube side outlet of the fixed bed reactor 1 connected with a tube side of the gas-gas heat exchanger 8, wherein the tube side outlet of the gas-gas heat exchanger 8 is connected with a shell side inlet of the hydrogen preheater 9, a shell side gas phase outlet of the hydrogen preheater 9 is connected with a shell side inlet of the cooler 10, and a shell side gas phase outlet of the cooler 10 is connected with the hydrogen buffer tank 14; the shell side liquid phase outlet of the hydrogen preheater 9 is connected to a product tank 18. The arrangement is designed based on normal production of the tube side of the fixed bed reactor 1 and treatment of the produced process gas, the process gas exchanges heat through the gas-gas heat exchanger 8, the hydrogen preheater 9 and the cooler 10, hydrogen can enter the hydrogen buffer tank 14 for repeated use, and the produced product enters the product tank 18. The shell side liquid phase outlet of the cooler 10 is connected to a water tank 16. The utility model shares a set of treatment device while treating the process gas, so that the conduction oil heat exchange unit for regulating and controlling the tube side temperature of the fixed bed reactor 1 is coupled, thereby realizing the recovery of the reduced water and the reutilization of the hydrogen in the reduction and heating stage of the catalyst.
Further, the outlet of the hydrogen buffer tank 14 is connected with a first tee joint 23 through the tube side of the hydrogen preheater 9 and the shell side of the gas-gas heat exchanger 8, the second end of the first tee joint 23 is connected with a second tee joint 24 through a third valve 20, and the third end of the first tee joint is connected with a vaporizer in the raw material pretreatment system 21 through a fourth valve 19; the second tee 24 is arranged between the gas phase outlet of the raw material pretreatment system 21 and the tube side of the fixed bed reactor 1, and a fifth valve 25 is arranged between the raw material pretreatment system 21 and the second tee 24. Through the arrangement, the original reduction heating of the catalyst is matched with the normal driving operation, so that the investment cost is reduced, the resistance of pipeline equipment in the driving stage can be reduced, and the purpose of reducing the power consumption of the hydrogen compressor is achieved.
Further, a hydrogen on-line analyzer 11 and a hydrogen compressor 12 are arranged between the shell side gas phase outlet of the cooler 10 and a hydrogen buffer tank 14, and the inlet of the hydrogen buffer tank 14 is also connected with a hydrogen pipeline 13. The hydrogen content can be detected by arranging the hydrogen on-line analyzer 11 so as to determine the nodes of each period of the catalyst reduction heating stage and provide a basis for the time of supplementing fresh hydrogen.
Further, a sixth valve 17 is arranged between the shell side liquid phase outlet of the hydrogen preheater 9 and the product tank 18.
Further, a seventh valve 15 is provided between the shell side liquid phase outlet of the cooler 10 and the water tank 16.
Further, the vaporizer inlet in the feedstock pretreatment system 21 is connected to a furfural storage tank 22.
The working principle of the utility model is as follows: the hydrogenation catalyst is filled in the tube pass of the fixed bed reactor 1, the catalyst in the fixed bed reactor 1 is reduced by hydrogen through a third valve 20, the shell pass of the fixed bed reactor 1 is connected with a heat conducting oil pump 7, heat conducting oil passes through a first valve 2, a heat conducting oil heater 4 or a second valve 3 and a steam drum 5 after transferring heat in the fixed bed reactor 1, and then enters a heat conducting oil storage tank 6, in the starting heating stage, the heat conducting oil is heated by the heat conducting oil heater 4 and the bed layer of the fixed bed reactor 1 is heated to a specific temperature, in the heat preservation stage, the heat conducting oil is cooled by the steam drum 5 and circularly enters the shell pass of the fixed bed reactor 1 through the heat conducting oil pump 7 to absorb reaction heat; the outlet process gas of the fixed bed reactor 1 sequentially passes through a gas heat exchanger 8, a hydrogen preheater 9 and a cooler 10, a seventh valve 15 is opened, a sixth valve 17 is closed, catalyst reduction effluent enters a water tank 16 for metering, the process gas is cooled and separated into liquid, then the liquid is analyzed by an online analyzer 11, and then the hydrogen content is boosted by a hydrogen compressor 12 and enters a hydrogen buffer tank 14 together with fresh hydrogen 13. The outlet hydrogen of the hydrogen buffer tank 14 is heated by the hydrogen preheater 9 and the gas heat exchanger 8 in sequence, and enters the fixed bed reactor 1 through the third valve 20. The heating reduction stage is finished, the starting feeding stage is started, the third valve 20 is closed, the fourth valve 19 is opened, hydrogen enters the raw material pretreatment system 21 to vaporize the furfural from the furfural storage tank 22, and the raw material pretreatment system comprises a vaporizer, a circulating pump, a superheater and other devices. Mixed raw material gas at an outlet of the raw material pretreatment system 21 enters the fixed bed reactor 1 through a fifth valve 25 and a second tee joint 24 to carry out hydrogenation reaction, the first valve 2 is closed, the second valve 3 is opened, and heat transfer oil circularly removes heat among a heat transfer oil storage tank 6, a heat transfer oil pump 7, the fixed bed reactor 1 and a steam drum 5; the outlet process gas of the fixed bed reactor 1 sequentially passes through the gas-gas heat exchanger 8, the hydrogen preheater 9 and the cooler 10, the seventh valve 15 is closed, the sixth valve 17 is opened, and shell side liquid of the hydrogen preheater 9 and the cooler 10 enters the product tank 18.
The utility model relates to a fast starting system for a fixed bed furfural hydrogenation reaction, which comprises the following steps when in specific use: step 1: the hydrogenation catalyst is filled in the tube side of the fixed bed reactor 1, and the catalyst in the fixed bed reactor 1 is reduced by the hydrogen from the second hydrogen valve 20. The active component of the hydrogenation catalyst is copper element, and the carrier is metal oxide such as silicon dioxide, calcium oxide and the like. The catalyst also needs nitrogen replacement operation before heating and reduction. The system pressure of the hydrogenation reduction stage of the catalyst is 20-50kpa. Step two: the shell side of the fixed bed reactor 1 is connected with a heat conduction oil pump 7, and the heat conduction oil passes through a first valve 2, a heat conduction oil heater 4 or a second valve 3 and a steam drum 5 after transferring heat in the fixed bed reactor 1 and enters a heat conduction oil storage tank 6. In the catalyst reduction heating stage, the heat-conducting oil is heated by a heat-conducting oil heater 4 and the bed layer of the fixed bed reactor 1 is heated to a specific temperature, and in the heat-preserving stage, the heat-conducting oil is cooled by a steam drum 5 and circularly enters the fixed bed reactor 1 by a heat-conducting oil pump 7 to absorb reaction heat. The reduction and heating stage of the catalyst is divided into an initial stage, a main stage, a later stage and a final stage; the initial fixed bed reactor 1 is heated from room temperature to 150-170 ℃ and the hydrogen content of the on-line analyzer 11 is 0%. The temperature of the fixed bed reactor 1 in the main period is 170-210 ℃, the temperature of 5-10 ℃ is a heating period, the temperature is kept for 1-8 hours in one period, and the hydrogen content of the online analyzer 11 is 1-6%. The temperature of the fixed bed reactor 1 in the later period is 210-240 ℃, the temperature of 10-15 ℃ is a heating period, the temperature is kept for 1-8 hours in one period, and the hydrogen content of the online analyzer 11 is 6-20%. The temperature of the final fixed bed reactor 1 is reduced from 240 ℃ to the reaction required temperature of 110-170 ℃, the temperature is reduced at uniform speed, and the hydrogen content of the online analyzer 11 is 80% -100%. Step 3: the outlet process gas of the fixed bed reactor 1 sequentially passes through the tube pass of the gas-gas heat exchanger 8, the shell pass of the hydrogen preheater 9 and the shell pass of the cooler 10, the seventh valve 15 is opened, the sixth valve 17 is closed, and the catalyst reduction effluent enters the water tank 16 for metering. The cooler 10 comprises a circulating water cooler and a chilled water cooler, wherein the cooler 10 is provided with a cold medium tube pass and a process gas shell pass. Step 4: after the temperature of the process gas is reduced and the liquid is separated, the hydrogen content is analyzed by an online analyzer 11, and then the hydrogen content is boosted by a hydrogen compressor 12 and enters a hydrogen buffer tank 14 together with fresh hydrogen from a hydrogen pipeline 13. The outlet pressure of the hydrogen compressor 12 is 45-100kpa. The outlet hydrogen of the hydrogen buffer tank 14 sequentially passes through the tube side of the hydrogen preheater 9 and the shell side of the gas heat exchanger 8 to heat, and enters the tube side of the fixed bed reactor 1 through the third valve 20, and at the moment, the fourth valve 19 is closed. Step 5: the temperature rise reduction stage is ended and enters a normal driving operation stage; the third valve 20 is closed and the fourth valve 19 is opened. Hydrogen enters the feed pretreatment system 21 to vaporize furfural from the furfural storage tank 22 with the hydrogen: the molar ratio of the furfural is 4-20:1. the raw material pretreatment system 21 comprises a vaporizer, a circulating pump, a superheater and the like. Step 6: the mixed feed gas at the outlet of the feed pretreatment system 21 enters the fixed bed reactor 1 to carry out hydrogenation reaction. The first valve 2 is closed, the second valve 3 is opened, and heat conduction oil is circulated among the heat conduction oil storage tank 6, the heat conduction oil pump 7, the fixed bed reactor 1 and the steam drum 5. Step 7: the outlet process gas of the fixed bed reactor 1 sequentially passes through a gas-gas heat exchanger 8, a hydrogen preheater 9 and a cooler 10; the seventh valve 15 is closed and the sixth valve 1717 is opened and the shell side liquid products of the hydrogen preheater 9 and the cooler 10 enter the product tank 18. The utility model can improve the temperature control speed, stably raise and lower the temperature, reduce the temperature fluctuation of the fixed bed reactor 1, ensure the quick and stable starting of the hydrogenation reaction of the fixed bed furfural, and can also reach the activation temperature of the catalyst faster, thereby reducing the generation of unqualified products on the basis of shortening the starting time; simultaneously, the full-load operation time from the reduction heating stage to the normal driving operation stage of the catalyst can be shortened to be within 72 hours by using the process.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. The utility model provides a quick driving system of fixed bed furfural hydrogenation, includes raw materials pretreatment systems (21), and the gas phase export of raw materials pretreatment systems (21) links to each other with the tube side of fixed bed reactor (1), and the tube side intussuseption of fixed bed reactor (1) is filled with catalyst layer, its characterized in that: the shell side outlet of the fixed bed reactor (1) is connected with a heat conducting oil storage tank (6) through a heat conducting oil heat exchange unit, and a heat conducting oil pump (7) of the heat conducting oil storage tank (6) is connected with the shell side inlet of the fixed bed reactor (1);
the heat conduction oil heat exchange unit comprises a heating part and a cooling part which are arranged in parallel.
2. The fast start-up system for hydrogenation reaction of furfural in a fixed bed according to claim 1, wherein: the heating part comprises a heat conduction oil heater (4) with a first valve (2) at the inlet.
3. The fast start-up system for hydrogenation reaction of furfural in a fixed bed according to claim 1, wherein: the cooling part comprises a steam drum (5) with a second valve (3) at the inlet for generating steam.
4. A fast start-up system for hydrogenation reactions of furfural in a fixed bed according to any one of claims 1-3, characterized in that: the device also comprises a tube side outlet connected with the fixed bed reactor (1) and a tube side of the gas-gas heat exchanger (8), wherein the tube side outlet of the gas-gas heat exchanger (8) is connected with a shell side inlet of the hydrogen preheater (9), a shell side gas phase outlet of the hydrogen preheater (9) is connected with a shell side inlet of the cooler (10), and a shell side gas phase outlet of the cooler (10) is connected with the hydrogen buffer tank (14);
the shell side liquid phase outlet of the hydrogen preheater (9) is connected with a product tank (18).
5. The fast starting system for the hydrogenation reaction of the fixed bed furfural of claim 4 is characterized in that: the shell side liquid phase outlet of the cooler (10) is connected with a water tank (16).
6. The fast starting system for the hydrogenation reaction of the fixed bed furfural of claim 4 is characterized in that: the outlet of the hydrogen buffer tank (14) is connected with a first tee joint (23) through a tube pass of the hydrogen preheater (9) and a shell pass of the gas-gas heat exchanger (8), the second end of the first tee joint (23) is connected with a second tee joint (24) through a third valve (20), and the third end of the first tee joint is connected with a vaporizer in the raw material pretreatment system (21) through a fourth valve (19);
the second tee joint (24) is arranged between a gas phase outlet of the raw material pretreatment system (21) and a tube side of the fixed bed reactor (1), and a fifth valve (25) is arranged between the raw material pretreatment system (21) and the second tee joint (24).
7. The fast starting system for the hydrogenation reaction of the fixed bed furfural of claim 4 is characterized in that: a hydrogen on-line analyzer (11) and a hydrogen compressor (12) are arranged between a shell side gas phase outlet of the cooler (10) and a hydrogen buffer tank (14), and an inlet of the hydrogen buffer tank (14) is also connected with a hydrogen pipeline (13).
8. The fast starting system for the hydrogenation reaction of the fixed bed furfural of claim 5 is characterized in that: a sixth valve (17) is arranged between the shell side liquid phase outlet of the hydrogen preheater (9) and the product tank (18).
9. The fast starting system for the hydrogenation reaction of the fixed bed furfural of claim 5 is characterized in that: a seventh valve (15) is arranged between the shell side liquid phase outlet of the cooler (10) and the water tank (16).
10. The fast start-up system for hydrogenation reaction of furfural in a fixed bed according to claim 1, wherein: the vaporizer inlet in the raw material pretreatment system (21) is connected with a furfural storage tank (22).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321127775.6U CN220026955U (en) | 2023-05-11 | 2023-05-11 | Fixed bed furfural hydrogenation reaction system of driving fast |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321127775.6U CN220026955U (en) | 2023-05-11 | 2023-05-11 | Fixed bed furfural hydrogenation reaction system of driving fast |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220026955U true CN220026955U (en) | 2023-11-17 |
Family
ID=88741361
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321127775.6U Active CN220026955U (en) | 2023-05-11 | 2023-05-11 | Fixed bed furfural hydrogenation reaction system of driving fast |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220026955U (en) |
-
2023
- 2023-05-11 CN CN202321127775.6U patent/CN220026955U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102185537B (en) | System and method for realizing cogeneration by using heat-conducting oil furnace and semiconductor power generation device | |
| CN104806311B (en) | Amino thermochemical energy-storage system | |
| CN106540639B (en) | Become gas low temperature exhaust heat recovery process in a kind of hydrocarbon steam conversion hydrogen production plant | |
| CN104826567B (en) | A kind of Cyclohexanone Production platinum catalysis hydrogenation heat energy is for the device of dehydrogenating technology | |
| CN101517795A (en) | Method and device for operating fuel cell used together with condenser | |
| CN220026955U (en) | Fixed bed furfural hydrogenation reaction system of driving fast | |
| CN109665527A (en) | The tail gas heat quantity recovery system and operation method of production of polysilicon equipment | |
| CN110793369B (en) | Supercritical water oxidation reaction product waste heat and residual pressure utilization system | |
| CN202400852U (en) | Polycrystalline silicon hydrogenation furnace tail gas energy saving system | |
| CN211012606U (en) | Supercritical water oxidation reaction product waste heat and residual pressure utilization system | |
| CN115264563A (en) | Heat storage peak regulation and energy-saving steam supply thermodynamic system | |
| CN212215471U (en) | Temperature adjusting system of reaction kettle | |
| CN210065193U (en) | Tail gas heat recovery system of polycrystalline silicon production equipment | |
| CN211204605U (en) | Heat exchange device of adsorption system | |
| CN204714766U (en) | A kind of methanation fluidized bed plant and methanation system | |
| CN219356168U (en) | Energy-saving production system for chloromethane | |
| CN219003025U (en) | Device capable of being used for producing 2-methyl furan or furfuryl alcohol | |
| CN211595468U (en) | Heat comprehensive utilization device in production process of acetyl n-propanol | |
| CN214496200U (en) | Middle section heat exchange system of hydrogenation fractionation equipment | |
| CN112759505A (en) | Method and system for preparing ethylene glycol | |
| CN220772003U (en) | Chemical energy storage system | |
| CN211051496U (en) | Reaction device | |
| CN201415980Y (en) | Energy saving heat exchange device | |
| CN215312202U (en) | Coal tar hydrogenation reaction feeding temperature control device | |
| CN215809432U (en) | Waste heat recovery utilizes device in concentrated nitric acid production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |