CN208517306U - Methanol-to-olefins system - Google Patents
Methanol-to-olefins system Download PDFInfo
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- CN208517306U CN208517306U CN201820745543.XU CN201820745543U CN208517306U CN 208517306 U CN208517306 U CN 208517306U CN 201820745543 U CN201820745543 U CN 201820745543U CN 208517306 U CN208517306 U CN 208517306U
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- methanol
- olefins
- gas
- stripping gas
- transfer pipeline
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 200
- 238000012546 transfer Methods 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 150000001336 alkenes Chemical class 0.000 claims abstract description 19
- 230000007246 mechanism Effects 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 110
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 54
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 54
- 239000004571 lime Substances 0.000 claims description 54
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 41
- 239000000126 substance Substances 0.000 claims description 18
- 238000003860 storage Methods 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000008213 purified water Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 9
- 238000012360 testing method Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 3
- 230000001112 coagulating effect Effects 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 18
- 230000008569 process Effects 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000012071 phase Substances 0.000 description 24
- 239000003245 coal Substances 0.000 description 8
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- -1 ethylene, propylene Chemical group 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000012545 processing Methods 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000004230 steam cracking Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 230000002459 sustained effect Effects 0.000 description 1
Classifications
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a kind of methanol-to-olefins system.The methanol-to-olefins system includes methanol to olefins reaction device, gas-phase methanol feeding mechanism and the first stripper plant, methanol to olefins reaction device is provided with feed opening, gas-phase methanol feeding mechanism is connected with feed opening by gas-phase methanol transfer pipeline, first stripper plant is provided with the outlet of the first stripping gas, and the outlet of the first stripping gas is connected with feed opening by the first stripping gas transfer pipeline.Directly it is connected with feed opening by the first stripping gas transfer pipeline by adding from the outlet of the first stripping gas, can will be fed directly in methanol to olefins reaction device from the methanol stripping gas exported in stripper.This, which can be saved, carries out stripping gas the processes such as to cool down, be concentrated, re-vaporize, so as to greatly save energy consumption.
Description
Technical field
The utility model relates to methanol-to-olefins fields, in particular to a kind of methanol-to-olefins system.
Background technique
With the sustained and rapid development of China's industrial or agricultural economy, needs of the market to basic organics such as ethylene, propylene
It is increasing.China's ethylene and most of propylene are relied primarily on using naphtha, steam cracking that light diesel fuel is raw material and are produced,
Part propylene is to be obtained by the oil liquefied gas of catalytic cracking by-product through rectifying processing.But due to the shortage of petroleum resources,
The reasons such as steam cracking scarce capacity, always supply falls short of demand for a long time for the ethylene yield in China, propylene yield, thus with second
Alkene, production of propylene the import volume of chemicals (such as polyethylene, polypropylene, ethylene glycol etc.) can not have always been high any more.In order to drop
The import rate of low external commercial opens in China and coal etc. is used to produce methanol for raw material, then methanol is raw through catalyzed conversion
Produce the new page of the light olefins such as ethylene, propylene.Methanol is the staple product and intermediate of Modern Coal-based Chemical, is connection coal chemical industry
With the main tie of refined oil product and chemical industry.The enlargement and product scale of methyl alcohol product installation will become Development of Coal Chemical Industry
Important feature.The necessarily choosing that coal becomes through methanol-to-olefins and develops Modern Coal-based Chemical industry, realizes national " with coal for replacing oil " strategy
It selects, technical bottleneck is methanol-to-olefins (MTO) technology.
The charging of methanol-to-olefins (MTO) device is the methanol after overheat, and general flow setting is that tank field methanol passes through
Successively enter reactor after heating, vaporization, overheat after pump pressurization to be reacted.Since the conversion ratio of reaction is not up to
100%, the oxides such as some unreacted methanol and dimethyl ether in the product gas after reaction.As reaction gas enters chilling
Tower and water scrubber, this partial oxide can enter in chilled water (chw) and washing water.In order to utilize the water of MTO device by-product, it is necessary to
Oxide in chilled water (chw) and washing water is reduced to acceptable range, is then provided with Wastewater Stripping Tower.As shown in Figure 1, will
Part chilled water (chw) and washing water are sent into Wastewater Stripping Tower 30 ', which is provided with reboiler, and the tube side of reboiler is passed through steam, will
Water into Wastewater Stripping Tower heats.Upstream device can be sent into after the COD (COD) of the purified water of tower bottom is up to standard to match
Coal uses, and is recycled after can also being sent into sewage-treatment plant processing.The stripping gas of tower top passes through methanol-stripping gas heat exchanger
60 ' and stripping Gas Cooler 50 ' it is cooling after, be conveyed into tower top lime set tank 40 '.It is flashed, is obtained not in tower top lime set tank 40 '
Solidifying gas and condensed water.Fixed gas is sent into methanol to olefins reaction device 10 ' and carries out freshening or feeding flare system, tower top lime set
Liquid (condensed water) in tank 40 ' is rich in oxides such as methanol, dimethyl ether.Condensed water is sent out through 70 ' a part of lime set delivery pump
Device battery limit (BL), a part are sent after overflash, overheat after mixing with the Liquid Phase Methanol raw material that gas-phase methanol feeding mechanism 20 ' provides
Enter methanol to olefins reaction device 10 '.
Existing MTO technology there are the problem of for existing MTO device condensed water freshening process it is longer, i.e. vapour
Mention gas after supercooling again in the form of condensed water with Liquid Phase Methanol converge after be vaporized again, overheat after be sent into reactor.Vapour
Gas originally gaseous phase materials are mentioned, are vaporized again after cooling, such flow setting has energy dissipation.
Utility model content
The main purpose of the utility model is to provide a kind of methanol-to-olefins systems, are deposited with solving existing MTO device
In the longer problem of condensed water freshening process.
To achieve the goals above, one aspect according to the present utility model provides a kind of methanol-to-olefins system, first
Alcohol alkene system includes methanol to olefins reaction device, gas-phase methanol feeding mechanism and the first stripper plant, methanol-to-olefins
Reaction unit is provided with feed opening, and gas-phase methanol feeding mechanism is connected with feed opening by gas-phase methanol transfer pipeline, and first
Stripper plant is provided with the outlet of the first stripping gas, and the outlet of the first stripping gas is connected with feed opening by the first stripping gas transfer pipeline
It is logical.
Further, methanol-to-olefins system further includes flowmeter, and flowmeter is arranged on the first stripping gas transfer pipeline.
Further, methanol-to-olefins system further include: stripping tower top lime set storage device and cooling device strip tower top
Lime set storage device is provided with lime set entrance and fixed gas outlet, and lime set entrance and the outlet of the first stripping gas pass through the second stripping gas
Transfer pipeline is connected, and fixed gas outlet is connected with feed opening；And cooling device is arranged on the second stripping gas transfer pipeline.
Further, methanol-to-olefins system further includes heat-exchanger rig, and heat-exchanger rig is for making gas-phase methanol transfer pipeline
In material exchange heat with the material in the second stripping gas transfer pipeline.
Further, methanol-to-olefins system further includes device for detecting chemical oxygen demand, and device for detecting chemical oxygen demand is used
In the COD for the purified water for detecting the first stripper plant outlet.
Further, methanol-to-olefins system further includes the second stripper plant, and the second stripper plant is provided with phegma and enters
Mouth and the outlet of the second stripping gas, stripping tower top lime set storage device are additionally provided with condensate outlet, condensate outlet and phegma entrance
It is connected by lime set transfer pipeline, and is located at heat-exchanger rig along the flow direction of gas-phase methanol, gas-phase methanol transfer pipeline
Part between gas-phase methanol feeding mechanism is connected.
Further, methanol-to-olefins system further includes lime set delivery pump, and lime set delivery pump is arranged in lime set transfer pipeline
On.
Further, methanol-to-olefins system further includes reversal valve, and the first stripping gas transfer pipeline and the second stripping gas are defeated
Pipeline is sent to switch over by reversal valve；When the testing result of device for detecting chemical oxygen demand is not up to standard, reversal valve has the
One position, the first stripping gas transfer pipeline are opened；When the testing result of device for detecting chemical oxygen demand is up to standard, reversal valve has
The second position, the second stripping gas transfer pipeline are opened.
Further, methanol-to-olefins system further includes drawing valve, draws valve and is arranged on the first stripping gas transfer pipeline,
And it is located at the upstream of flowmeter.
Further, methanol-to-olefins system further includes check valve, and check valve, which is arranged in, draws between valve and flowmeter
On flow path.
Using the technical solution of the utility model, in methanol-to-olefins system, exported by adding from the first stripping gas
Directly it is connected with feed opening by the first stripping gas transfer pipeline, it can be direct by the methanol stripping gas exported from stripper
It is delivered in methanol to olefins reaction device.This, which can be saved, carries out stripping gas the processes such as to cool down, be concentrated, re-vaporize, thus
Energy consumption can be greatlyd save.
Detailed description of the invention
The accompanying drawings constituting a part of this application is used to provide a further understanding of the present invention, this is practical
Novel illustrative embodiments and their description are not constituteed improper limits to the present invention for explaining the utility model.
In the accompanying drawings:
Fig. 1 shows the structural schematic diagram of existing methanol-to-olefins system；
Fig. 2 shows a kind of structures for the methanol-to-olefins system that typical embodiment provides according to the present utility model
Schematic diagram.
Wherein, the above drawings include the following reference numerals:
10 ', methanol to olefins reaction device；20 ', gas-phase methanol feeding mechanism；30 ', Wastewater Stripping Tower；40 ', tower top lime set
Tank；50 ', Gas Cooler is stripped；60 ', methanol-stripping gas heat-exchanger rig heat exchanger；70 ', lime set delivery pump；
10, methanol to olefins reaction device；20, gas-phase methanol feeding mechanism；30, the first stripper plant；31, flowmeter；
32, valve is drawn；33, check valve；34, blow valve；35, showering guilding valve；36, bottom valve；301, the first stripping gas exports；40, it strips
Tower top lime set storage device；401, lime set entrance；402, fixed gas exports；403, condensate outlet；50, cooling device；60, it exchanges heat
Device；70, device for detecting chemical oxygen demand；80, the second stripper plant；801, phegma entrance；802, the second stripping gas exports；
90, lime set delivery pump.
Specific embodiment
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.The utility model is described in detail below in conjunction with embodiment.
As described in background technique, there are the longer problems of condensed water freshening process for existing MTO device.To understand
Certainly above-mentioned technical problem, this application provides a kind of methanol-to-olefins systems, as shown in Fig. 2, the methanol-to-olefins system includes
Methanol to olefins reaction device 10, gas-phase methanol feeding mechanism 20 and the first stripper plant 30, methanol to olefins reaction device 10
It is provided with feed opening, gas-phase methanol feeding mechanism 20 is connected with feed opening by gas-phase methanol transfer pipeline, the first stripping dress
It sets 30 and is provided with the first stripping gas outlet 301, the first stripping gas outlet 301 passes through the first stripping gas transfer pipeline phase with feed opening
Connection.
In methanol-to-olefins system provided by the present application, by adding from the first stripping gas outlet 301 directly and feed opening
It is connected by the first stripping gas transfer pipeline, the methanol stripping gas exported from stripper can be fed directly to methanol system
In olefine reaction device 10.This, which can be saved, carries out stripping gas the processes such as to cool down, be concentrated, re-vaporize, so as to save significantly
About energy consumption.
Energy consumption can be greatlyd save using above-mentioned methanol-to-olefins device.In a kind of preferred embodiment, such as Fig. 2 institute
Show, methanol-to-olefins system further includes flowmeter 31, and flowmeter 31 is arranged on the first stripping gas transfer pipeline.Above-mentioned first
Flowmeter 31 is arranged on stripping gas transfer pipeline can accurately control the flow of stripping gas in the first stripping gas transfer pipeline.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes stripping tower top lime set storage dress
Set 40 and cooling device 50.Stripping tower top lime set storage device 40 is provided with lime set entrance 401 and fixed gas outlet 402, lime set
Entrance 401 is connected with the first stripping gas outlet 301 by the second stripping gas transfer pipeline, fixed gas outlet 402 and feed opening
It is connected；And cooling device 50 is arranged on the second stripping gas transfer pipeline.
The setting stripping tower top lime set storage device 40 and cooling device 50 in above-mentioned methanol-to-olefins system, can will be from
The methanol gas being stripped off in methanol-to-olefins system is cooled down, and is then flashed in stripping tower top lime set storage device 40,
Obtain fixed gas and condensed water.Fixed gas can be passed directly into the feed opening of methanol to olefins reaction device 10, as reaction
Raw material.And condensed water can carry out stripping processing again.
Preferably, as shown in Fig. 2, methanol-to-olefins system further includes heat-exchanger rig 60, the setting of heat-exchanger rig 60 can
Material and the material in the second stripping gas transfer pipeline in gas-phase methanol transfer pipeline is set to exchange heat, to be conducive to improve
The utilization rate of the energy in entire methanol-to-olefins system.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes the second stripper plant 80, the
Two stripper plants 80 are provided with phegma entrance 801 and the second stripping gas outlet 802, and stripping tower top lime set storage device 40 is also set
It is equipped with condensate outlet 403, condensate outlet 403 is connected with phegma entrance 801 by lime set transfer pipeline, along gas-phase methanol
Flow direction, and the part in gas-phase methanol transfer pipeline between heat-exchanger rig 60 and gas-phase methanol feeding mechanism 20 is connected
It is logical.
The lime set for stripping tower top lime set storage device 40 is stripped again by the second stripper plant 80, obtains the
Two stripping gases, and pass through 802 discharge of the second stripping gas outlet.By the first of the second stripping gas outlet 802 and 60 upstream of heat-exchanger rig
Alcohol transfer pipeline is connected to, this can carry out circulation benefit again for the lime set for stripping tower top as the raw material of methanol-to-olefins
With to advantageously reduce cost of material.
Simultaneously in order to save the process cost, can also will from stripping tower top lime set storage device 40 condensed water that flash off
It is fed directly to be stripped in the first stripper plant 30.
The first stripping gas transfer pipeline and the second lime set transfer pipeline are existed simultaneously in above-mentioned methanol-to-olefins system, due to
Methanol stripping gas can directly be utilized without condensation process by the first stripping gas transfer pipeline, this eliminate by
Methanol stripping gas carries out the process of cooling re-vaporization, to significantly reduce the consumption of the energy.In a kind of preferred embodiment,
As shown in Fig. 2, methanol-to-olefins system further includes device for detecting chemical oxygen demand 70, which is used for
Detect the COD of the purified water of 30 outlet of the first stripper plant.
The COD of the purified water of 30 outlet of the first stripper plant is detected by device for detecting chemical oxygen demand 70
(COD), the processing mode to the first stripping gas is then determined according to testing result.Specifically, when the COD of methanol stripping gas does not reach
When mark, methanol stripping gas is delivered in methanol to olefins reaction device 10 from the first stripping gas transfer pipeline；And work as methanol vapor
Mention gas COD it is up to standard when, methanol stripping gas is delivered in methanol to olefins reaction device 10 from the second stripping gas transfer pipeline.
This not only contributes to the raising feature of environmental protection can also energy saving.
Preferably, above-mentioned methanol-to-olefins system further includes reversal valve, and the second lime set pipeline passes through with the first lime set pipeline
Reversal valve switches over, and when the testing result of device for detecting chemical oxygen demand 70 is not up to standard, reversal valve has first position, the
One stripping gas transfer pipeline is opened；When the testing result of device for detecting chemical oxygen demand 70 is up to standard, reversal valve has second
It sets, the second stripping gas transfer pipeline is opened.
Preferably, as shown in Fig. 2, methanol-to-olefins system further includes lime set delivery pump 90, the setting of lime set delivery pump 90 exists
On lime set transfer pipeline.The delivery rate that lime set delivery pump 90 is conducive to improve lime set is set.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes drawing valve 32, valve 32 is drawn
It is arranged on the first stripping gas transfer pipeline, and is located at the upstream of flowmeter 31.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes check valve 33, check valve 33
It is arranged on the flow path drawn between valve 32 and flowmeter 31.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes blow valve 34, blow valve 34
It is arranged on the flow path between check valve 33 and flowmeter 31.
In a kind of preferred embodiment, as shown in Fig. 2, methanol-to-olefins system further includes showering guilding valve 35 and line end
Valve 36, showering guilding valve 35 and line end valve 36 are arranged on the first stripping gas transfer pipeline, and are located at the downstream of flowmeter 31.
The application is described in further detail below in conjunction with specific embodiment, these embodiments should not be understood as limitation originally
Apply for range claimed.
Embodiment 1
As shown in Fig. 2, waste water is stripped through the first stripper plant 30 (stripper) when the purified water COD sent outside is up to standard
To stripping gas.Above-mentioned stripping gas is after heat-exchanger rig 60 and cooling device 50 are exchanged heat and cooled down, into stripping tower top lime set
Storage device 40 (stripping tower top lime set tank).In stripping tower top lime set storage device 40, the stripping gas of saturation is laggard through flashing
Row gas-liquid separation obtains fixed gas and stripping tower top lime set (condensed water).Enter first after fixed gas and gas-phase methanol are converged simultaneously
Alcohol olefine reaction device 10 carries out freshening.Stripping tower top lime set (condensed water) then returns to second after the boosting of lime set delivery pump 90
It is stripped again in stripper plant 80.
When the purified water COD sent outside is exceeded, the first stripping gas transfer pipeline is opened immediately.Specifically, waste water is by the
One stripper plant 30 is stripped to obtain the first stripping gas.Then the first stripping gas without heat exchange is through the first stripping letter shoot
After extraction valve 32, check valve 33, flowmeter 31 (orifice flowmeter) and bottom valve 36 in road, then with gas-phase methanol feeding mechanism
20 gas-phase methanols provided are directly entered methanol to olefins reaction device 10 after converging and are reacted.As the purified water COD sent outside
When index is restored to normal value, stripping gas freshening can be stopped, closing the extraction valve on the first newly-increased stripping gas transfer pipeline
32 and bottom valve 36, the blow valve 34 before opening flowmeter 31 carries out pressure release.
Stripping gas can be eliminated through exchanging heat when the purified water COD sent outside is exceeded using above-mentioned methanol-to-olefins system
After device 60 is cooling, the process cooled down again through cooling device 50 reduces equipment investment, operation expense, reduces vapour
Propose the energy consumption of gas secondary cooling；Meanwhile it eliminating stripping tower top lime set (condensed water) and carrying out the process of freshening, stripping tower top lime set
(condensed water) reduces the energy consumption that condensed water is handled outside concentration water vapor and device to battery limit (BL) process.
It can be seen from the above description that the above embodiments of the utility model achieve the following technical effects:
(1) stripping gas reduces energy consumption when stripping gas is cooled to condensed water with gas phase freshening.
(2) stripping gas is heated, the energy consumption of vaporization condensed water with gas phase freshening when reducing condensed water freshening.
(3) stripping gas freshening process using flexible decides whether the process that comes into operation according to COD content in purified water.It uses
Stripping gas freshening method, the purified water only COD up to standard of carrying device, no condensed water carrying device reduce subsequent place
Manage cost.Using stripping gas freshening method, unconverted methanol, dimethyl ether recycle in the device, and no condensed water is sent outside, reduce
The loss of material.
The above descriptions are merely preferred embodiments of the present invention, is not intended to limit the utility model, for this
For the technical staff in field, various modifications and changes may be made to the present invention.It is all in the spirit and principles of the utility model
Within, any modification, equivalent replacement, improvement and so on should be included within the scope of protection of this utility model.
Claims (10)
1. a kind of methanol-to-olefins system, which is characterized in that the methanol-to-olefins system includes:
Methanol to olefins reaction device (10), the methanol to olefins reaction device (10) are provided with feed opening；
Gas-phase methanol feeding mechanism (20), the gas-phase methanol feeding mechanism (20) and the feed opening are conveyed by gas-phase methanol
Pipeline is connected；
First stripper plant (30), first stripper plant (30) are provided with the first stripping gas outlet (301), first vapour
Gas outlet (301) is proposed to be connected with the feed opening by the first stripping gas transfer pipeline.
2. methanol-to-olefins system according to claim 1, which is characterized in that the methanol-to-olefins system further includes stream
Meter (31), the flowmeter (31) are arranged on the first stripping gas transfer pipeline.
3. methanol-to-olefins system according to claim 1 or 2, which is characterized in that the methanol-to-olefins system is also wrapped
It includes:
It strips tower top lime set storage device (40), the stripping tower top lime set storage device (40) is provided with lime set entrance (401)
(402) are exported with fixed gas, the lime set entrance (401) and first stripping gas export (301) to pass through the second stripping gas defeated
Pipeline is sent to be connected, the fixed gas outlet (402) is connected with the feed opening；And
Cooling device (50), the cooling device (50) are arranged on the second stripping gas transfer pipeline.
4. methanol-to-olefins system according to claim 3, which is characterized in that the methanol-to-olefins system further includes changing
Thermal (60), the heat-exchanger rig (60) are used to make material and second stripping gas in the gas-phase methanol transfer pipeline
Material in transfer pipeline exchanges heat.
5. methanol-to-olefins system according to claim 4, which is characterized in that the further including of methanol-to-olefins system
It learns aerobic amount detecting device (70), the device for detecting chemical oxygen demand (70) is for detecting first stripper plant (30) outside
The COD of the purified water of row.
6. methanol-to-olefins system according to claim 5, which is characterized in that the methanol-to-olefins system further includes
Two stripper plants (80), second stripper plant (80) are provided with phegma entrance (801) and the outlet of the second stripping gas
(802),
The stripping tower top lime set storage device (40) is additionally provided with condensate outlet (403), the condensate outlet (403) with it is described
Phegma entrance (801) is connected by lime set transfer pipeline, and second stripping gas outlet (802) and the gas-phase methanol
Part in transfer pipeline between the heat-exchanger rig (60) and the gas-phase methanol feeding mechanism (20) is connected.
7. methanol-to-olefins system according to claim 6, which is characterized in that the methanol-to-olefins system further includes coagulating
Liquid delivery pump (90), the lime set delivery pump (90) are arranged on the lime set transfer pipeline.
8. methanol-to-olefins system according to claim 7, which is characterized in that the methanol-to-olefins system further includes changing
To valve, the first stripping gas transfer pipeline is switched over the second stripping gas transfer pipeline by the reversal valve；When
When the testing result of the device for detecting chemical oxygen demand (70) is not up to standard, the reversal valve have first position, described first
Stripping gas transfer pipeline is opened；When the testing result of the device for detecting chemical oxygen demand (70) is up to standard, the reversal valve tool
There is the second position, the second stripping gas transfer pipeline is opened.
9. methanol-to-olefins system according to claim 2, which is characterized in that the methanol-to-olefins system further includes drawing
Valve (32) out, the extraction valve (32) are arranged on the first stripping gas transfer pipeline, and are located at the flowmeter (31)
Upstream.
10. methanol-to-olefins system according to claim 9, which is characterized in that the methanol-to-olefins system further includes
Check valve (33), check valve (33) setting is on the flow path between extraction valve (32) and the flowmeter (31).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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