CN105148986A - Methanol-to-olefin catalyst bed temperature rise and regeneration device - Google Patents
Methanol-to-olefin catalyst bed temperature rise and regeneration device Download PDFInfo
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Abstract
The invention particularly discloses a methanol-to-olefin catalyst bed temperature rise and regeneration device. The device comprises a heater, a reactor, a cooler, a carbon dioxide online monitor, a buffer tank, a Roots blower, an activation or regeneration gas main valve, a first-stage gas inlet control valve, a second-stage gas inlet control valve, a third-stage gas inlet control valve, a fourth-stage gas inlet control valve, a high-temperature gas diverter valve, a recycle gas pipeline hand valve, a first-stage gas flow meter, a second-stage gas flow meter, a third-stage gas flow meter, a fourth-stage gas flow meter and the like. According to the device, the workload of the cooler can be reduced, and energy consumption can be lowered; because the inlet temperature of the heater is increased to the maximum degree, the energy consumption of the heater is lowered, and the energy saving effect is achieved. From the perspective of increasing the resource utilization rate, part or all of catalyst bed temperature rise or regeneration gas is recycled instead of being completely emptied directly, and the design can save lots of catalyst bed temperature rise or regeneration gas and increase the resource utilization rate.
Description
Technical field
The present invention relates to molecular sieve is the fixed bde catalyst bed intensification of carrier or the device of regeneration, is specially methanol-to-olefin catalyst bed and heats up and regenerating unit.
Background technology
Take molecular sieve as the fixed bde catalyst of carrier, be widely used in industrial production, and be that the methanol-to-olefin catalyst of carrier is also applied gradually with ZSM-5 molecular sieve.Current employing fixed bed methanol-to-olefin catalyst bed heats up and regenerating unit technological process mainly contains one, be exactly beds heat up or regeneration gas after heating, pass into reactor, after acting on catalyst, all coolings, emptying.As shown in Figure 1, flow scheme design for existing beds intensification or regenerating unit is that beds heats up or regeneration gas, heat up or regeneration gas main valve V-1 through beds, enter heater 1 and be heated to beds intensification or regeneration temperature, heater 1 exports and one-level gas flowmeter F-1, secondary gas flowmeter F-2, three grades of gas flowmeter F-3, level Four gas flowmeter F-4 entrance is connected, flowmeter and corresponding one-level air intake control valve V-2, secondary inlet control valve V-3, three grades of air intake control valve V-4, level Four air intake control valve V-5 is communicated with, control valve outlet is connected with the beds at different levels of reactor 2, reactor 2 outlet is communicated with cooler 3, after gas cooling, by atmospheric valve V-6 emptying.This designs the beds that uses and heats up or after regeneration gas action catalysts, all cool emptying, and this design causes beds to heat up or the waste of regeneration gas, could not realize making full use of of resource and the energy.
Summary of the invention
The object of the invention is to for above technical problem, provide one fully can economize on resources, reduce thermal loss, promote that methanol-to-olefin catalyst bed heats up and regenerating unit.
The object of the invention is realized by following technical proposals:
Methanol-to-olefin catalyst bed heats up and regenerating unit, and this device comprises heater, reactor, cooler, carbon dioxide on-line computing model, surge tank, Roots blower, open and live or gas for regeneration main valve, one-level air intake control valve, secondary inlet control valve, three grades of air intake control valves, level Four air intake control valve, high-temperature gas flow divider, circulating air pipeline hand valve, one-level gas flowmeter, secondary gas flowmeter, three grades of gas flowmeters, level Four gas flowmeter, it opens lives or gas for regeneration main valve one end is communicated with calorifier inlets, the other end with open work or regenerate source of the gas and be connected, heater outlet respectively with one-level gas flowmeter, secondary gas flowmeter, three grades of gas flowmeters, level Four gas flowmeter entrance is communicated with, flowmeter at different levels and corresponding one-level air intake control valve, secondary inlet control valve, three grades of air intake control valves, level Four air intake control valve is communicated with, control valve outlet is connected with the beds at different levels of reactor, reactor outlet and high-temperature gas flow divider inlet communication, high-temperature gas flow divider exports a road and is connected with cooler entrance, another road and circulating air control to be communicated with surge tank entrance after main valve outlet line is communicated with again, surge tank outlet is communicated with Roots blower entrance, and Roots blower outlet is communicated with circulating air pipeline hand valve inlet, and circulating air pipeline hand valve outlet port is communicated with calorifier inlets.
This device also comprises atmospheric valve and circulating air controls main valve, and the entrance that cooler outlet controls main valve with atmospheric valve, circulating air is respectively communicated with, and atmospheric valve outlet is communicated with blow-down pipe.
This device also comprises mist temperature monitoring thermocouple, installs mist temperature detection thermocouple at surge tank entrance.
This device also comprises pressure transmitter, Roots blower outlet pipeline setting pressure transmitter.
Compared with prior art, beneficial effect of the present invention is:
(1) from Energy Angle, when beds heats up or regenerates, gas used is after catalyst, by high-temperature gas flow divider, one enters cooler cooling, and another part branches to pipeloop, with gas and vapor permeation after cooling, as long as the inlet temperature that mist temperature meets Roots blower requires, such one is the live load that can reduce cooler, reduces energy consumption; Two is because promote calorifier inlets temperature to greatest extent, thus reduces the energy ezpenditure of heater, reaches energy-saving effect.From the angle improving resource utilization, recycle some or all of beds and heat up or regeneration gas, instead of directly all by its emptying, this design can be saved a large amount of beds and be heated up or regeneration gas, improves the level of resources utilization.
(2) the design can according to each bed catalyst inactivation concrete condition, controls temperature and the consumption of gas during catalyst regeneration, reaches optimization regeneration scheme, realizes distributing rationally of the energy and resource.
Accompanying drawing explanation
Fig. 1 is traditional employing fixed bed methanol-to-olefin catalyst bed intensification and the process chart of regenerating unit.
Fig. 2 is the process chart of methanol-to-olefin catalyst bed of the present invention intensification and regenerating unit.
Wherein, 1---heater, 2---reactor, 3---cooler, 4---carbon dioxide on-line computing model, 5---mist temperature monitoring thermocouple, 6---surge tank, 7---Roots blower, 8---pressure transmitter, V-1---beds heats up or gas for regeneration main valve, V-2---one-level air intake control valve, V-3---secondary inlet control valve, V-4---three grades of air intake control valves, V-5---level Four air intake control valve, V-6---atmospheric valve, V-7---circulating air controls main valve, V-8---high-temperature gas flow divider, V-9---circulating air pipeline hand valve, F-1---one-level gas flowmeter, F-2---secondary gas flowmeter, F-3---three grades of gas flowmeters, F-4---level Four gas flowmeter.
Detailed description of the invention
All features disclosed in this description, or the step in disclosed all methods or process, except mutually exclusive feature and/or step, all can combine by any way.
Arbitrary feature disclosed in this description (comprising any accessory claim, summary), unless specifically stated otherwise, all can be replaced by other equivalences or the alternative features with similar object.That is, unless specifically stated otherwise, each feature is an example in a series of equivalence or similar characteristics.
As shown in Figure 2, methanol-to-olefins device beds heats up and regenerating unit, include heater 1, reactor 2, cooler 3, carbon dioxide on-line computing model 4, mist temperature monitoring thermocouple 5, surge tank 6, Roots blower 7, pressure transmitter 8, beds heats up or gas for regeneration main valve V-1, one-level air intake control valve V-2, secondary inlet control valve V-3, three grades of air intake control valve V-4, level Four air intake control valve V-5, atmospheric valve V-6, circulating air controls main valve V-7, high-temperature gas flow divider V-8, circulating air pipeline hand valve V-9, one-level gas flowmeter F-1, secondary gas flowmeter F-2, three grades of gas flowmeter F-3, level Four gas flowmeter F-4.
Beds heats up or gas for regeneration main valve V-1 one end is communicated with heater 1 entrance, and the other end heats up with beds or regenerates source of the gas and is connected.Heater 1 exports and one-level gas flowmeter F-1, secondary gas flowmeter F-2, three grades of gas flowmeter F-3, level Four gas flowmeter F-4 entrance is communicated with, flowmeter at different levels and corresponding one-level air intake control valve V-2, secondary inlet control valve V-3, three grades of air intake control valve V-4, level Four air intake control valve V-5 is communicated with, control valve outlet is connected with the beds at different levels of reactor 2, reactor 2 exports and high-temperature gas flow divider V-8 inlet communication, high-temperature gas flow divider V-8 exports a road and is connected with cooler 3 entrance, another road and circulating air control main valve V-7 outlet line and are communicated with, this Lu Yu surge tank 6 entrance is communicated with, surge tank 6 outlet is communicated with Roots blower 7 entrance, Roots blower 7 outlet is communicated with circulating air pipeline hand valve V-9 entrance, circulating air pipeline hand valve V-9 outlet is communicated with electric heater entrance, cooler 3 exports the entrance controlling main valve V-7 respectively with atmospheric valve V-6, circulating air and is communicated with, and atmospheric valve V-6 outlet is communicated with blow-down pipe, surge tank 6 entrance installs mist temperature monitoring thermocouple 5, Roots blower 7 outlet line setting pressure transmitter 8.
Embodiment 1:
When beds heats up, for the inert nitrogen gas heated up, heater 1 is entered by gas main valve V-1, gradually nitrogen is heated to 450 DEG C, high temperature nitrogen after heating controls by one-level air intake control valve V-2, secondary inlet control valve V-3, three grades of air intake control valve V-4, level Four air intake control valve V-5 the different catalysts bed that nitrogen enters reactor 2, and one-level gas flowmeter F-1, secondary gas flowmeter F-2, three grades of gas flowmeter F-3, level Four gas flowmeter F-4 measure gas flow at different levels respectively simultaneously; Nitrogen flows out after each bed of reactor 2, the high temperature nitrogen that reactor 2 exports is by high-temperature gas flow divider V-8, distribution of gas flows to cooler 3 and enters the gas flow of pipeloop, measured the gas that directly enters mixing line by high-temperature gas flow divider V-8 by mist temperature monitoring thermocouple in real time and control by circulating air the temperature that main valve V-7 enters the mist of pipeloop gas after cooler 3 cools, not higher than 200 DEG C, to meet the requirement of Roots blower 7 pairs of inlet temperatures.Mist enters Roots blower 7 supercharging 100kpa through surge tank 6, the pressure transmitter 8 gas-monitoring pressure exported by Roots blower 7, is circulated to heater 1 entrance afterwards through circulating air pipeline hand valve V-9.When reaction bed temperature reaches 400 DEG C, beds heats up and terminates.
Embodiment 2:
During catalyst regeneration, the mist be made up of nitrogen and air, according to the mixed proportion of volume ratio 4:1, enter heater 1 by gas main valve V-1, mist is heated to 550 DEG C, and the high-temperature gas mixture body after heating enters the different beds of reactor 2.Control by one-level air intake control valve V-2, secondary inlet control valve V-3, three grades of air intake control valve V-4, level Four air intake control valve V-5 the gas flow that mist enters reactor 2 different catalysts bed, one-level gas flowmeter F-1, secondary gas flowmeter F-2, three grades of gas flowmeter F-3, level Four gas flowmeter F-4 measure gas flow at different levels respectively; Mist flows out after each bed of reactor 2, and the mist that reactor 2 exports is by high-temperature gas flow divider V-8, and a part flows to cooler 3, another part and the gas and vapor permeation controlling main valve V-7 from circulating air; Flow to the high-temperature gas of cooler 3, be cooled to not higher than 60 DEG C, according to the testing result of carbon dioxide on-line computing model 4, judge that gas is emptying, still recycle.When the content of carbon dioxide is more than 2%, then turn or close high-temperature gas flow divider V-8 down to remove pipeloop, turn or close circulating air control main valve V-7 down, open atmospheric valve V-6, by evacuate air, open gas main valve V-1 simultaneously, supplement fresh regenerated gas to system, if the content of carbon dioxide lower than 2% time, then close atmospheric valve V-6, open circulating air and control main valve V-7, this strand of gas mixes with the high-temperature gas that high-temperature gas flow divider V-8 comes, the temperature of mist is monitored not higher than 200 DEG C by mist temperature monitoring thermocouple 5, to meet the requirement of Roots blower 7 pairs of inlet temperatures, after two strands of gas and vapor permeation, Roots blower 7 entrance is flowed to through surge tank 6, gas is after Roots blower 7 supercharging 100kpa, flow to circulating air pipeline hand valve V-9, thus flow back to heater 1 entrance, realize the recycling with partial heat that recycles of gas.
The beds that the present invention is not limited to methanol-to-olefins heats up and catalyst regeneration device.The present invention extend to molecular sieve be carrier fixed bde catalyst heat up or catalyst regeneration device.Also any new feature of disclosing in this manual or any combination is newly extended to, and the step of the arbitrary new method disclosed or process or any combination newly.
Claims (4)
1. methanol-to-olefin catalyst bed heats up and regenerating unit, and this device comprises heater, reactor, cooler, carbon dioxide on-line computing model, surge tank, Roots blower, open and live or gas for regeneration main valve, one-level air intake control valve, secondary inlet control valve, three grades of air intake control valves, level Four air intake control valve, high-temperature gas flow divider, circulating air pipeline hand valve, one-level gas flowmeter, secondary gas flowmeter, three grades of gas flowmeters, level Four gas flowmeter, is characterized in that: open and to live or gas for regeneration main valve one end is communicated with calorifier inlets, the other end with open work or regenerate source of the gas and be connected, heater outlet respectively with one-level gas flowmeter, secondary gas flowmeter, three grades of gas flowmeters, level Four gas flowmeter entrance is communicated with, flowmeter at different levels and corresponding one-level air intake control valve, secondary inlet control valve, three grades of air intake control valves, level Four air intake control valve is communicated with, control valve outlet is connected with the beds at different levels of reactor, reactor outlet and high-temperature gas flow divider inlet communication, high-temperature gas flow divider exports a road and is connected with cooler entrance, another road and circulating air control to be communicated with surge tank entrance after main valve outlet line is communicated with again, surge tank outlet is communicated with Roots blower entrance, and Roots blower outlet is communicated with circulating air pipeline hand valve inlet, and circulating air pipeline hand valve outlet port is communicated with calorifier inlets.
2. methanol-to-olefin catalyst bed according to claim 1 heats up and regenerating unit, it is characterized in that: this device also comprises atmospheric valve and circulating air controls main valve, the entrance that cooler outlet controls main valve with atmospheric valve, circulating air is respectively communicated with, and atmospheric valve outlet is communicated with blow-down pipe.
3. methanol-to-olefin catalyst bed according to claim 1 heats up and regenerating unit, it is characterized in that: this device also comprises mist temperature monitoring thermocouple, installs mist temperature detection thermocouple at surge tank entrance.
4. methanol-to-olefin catalyst bed according to claim 1 heats up and regenerating unit, it is characterized in that: this device also comprises pressure transmitter, Roots blower outlet pipeline setting pressure transmitter.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109701454A (en) * | 2019-01-28 | 2019-05-03 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation, which goes into operation, recycles heat riser |
| CN111185125A (en) * | 2020-01-08 | 2020-05-22 | 中国科学院工程热物理研究所 | Device and method for activating deactivated catalyst |
| CN113457748A (en) * | 2021-07-27 | 2021-10-01 | 北京石油化工工程有限公司 | Catalyst out-of-reactor regeneration system and method |
| CN114076318A (en) * | 2020-08-20 | 2022-02-22 | 中石化南京化工研究院有限公司 | Sulfur-containing waste treatment system, start-up temperature rise method, device and storage medium |
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| CN109701454A (en) * | 2019-01-28 | 2019-05-03 | 安庆市泰发能源科技有限公司 | Butane dehydrogenation, which goes into operation, recycles heat riser |
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| CN111185125A (en) * | 2020-01-08 | 2020-05-22 | 中国科学院工程热物理研究所 | Device and method for activating deactivated catalyst |
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| CN114076318A (en) * | 2020-08-20 | 2022-02-22 | 中石化南京化工研究院有限公司 | Sulfur-containing waste treatment system, start-up temperature rise method, device and storage medium |
| CN113457748A (en) * | 2021-07-27 | 2021-10-01 | 北京石油化工工程有限公司 | Catalyst out-of-reactor regeneration system and method |
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| CN105148986B (en) | 2017-10-20 |
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Effective date of registration: 20191216 Address after: 611436 No.777, Xinghua 10th Road, dengshuang Town, Xinjin County, Chengdu City, Sichuan Province (Industrial Park) Patentee after: HAO HUA (CHENGDU) TECHNOLOGY Co.,Ltd. Address before: No. 5 high tech Zone Gaopeng road in Chengdu city of Sichuan Province in 610225 Patentee before: SOUTHWEST RESEARCH & DESIGN INSTITUTE OF CHEMICAL INDUSTRY |
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