CN205740823U - A kind of MTP device - Google Patents
A kind of MTP device Download PDFInfo
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- CN205740823U CN205740823U CN201521130085.1U CN201521130085U CN205740823U CN 205740823 U CN205740823 U CN 205740823U CN 201521130085 U CN201521130085 U CN 201521130085U CN 205740823 U CN205740823 U CN 205740823U
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- 238000000034 method Methods 0.000 claims abstract description 39
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 34
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 97
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 67
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 61
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 61
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 60
- 239000013505 freshwater Substances 0.000 claims description 40
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- 239000007788 liquid Substances 0.000 claims description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 12
- 239000007792 gaseous phase Substances 0.000 claims description 11
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- 239000003518 caustics Substances 0.000 claims description 10
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 8
- 230000000171 quenching effect Effects 0.000 claims description 8
- 238000006396 nitration reaction Methods 0.000 claims description 7
- 238000005354 coacervation Methods 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 238000005342 ion exchange Methods 0.000 claims description 5
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- -1 alcohols organic oxygen compound Chemical class 0.000 claims description 4
- 239000003599 detergent Substances 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
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- 210000000952 spleen Anatomy 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims description 3
- 150000007524 organic acids Chemical class 0.000 claims description 3
- 235000019628 coolness Nutrition 0.000 claims description 2
- 239000002737 fuel gas Substances 0.000 abstract description 14
- 239000006227 byproduct Substances 0.000 abstract description 10
- 239000000463 material Substances 0.000 abstract description 10
- 230000006835 compression Effects 0.000 abstract description 9
- 238000007906 compression Methods 0.000 abstract description 9
- 239000012495 reaction gas Substances 0.000 abstract description 8
- 239000003513 alkali Substances 0.000 abstract description 4
- 238000004140 cleaning Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000005457 optimization Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 28
- 238000005516 engineering process Methods 0.000 description 12
- 238000000746 purification Methods 0.000 description 7
- 230000002745 absorbent Effects 0.000 description 6
- 239000002250 absorbent Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
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- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 150000004831 organic oxygen compounds Chemical class 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
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- 239000002808 molecular sieve Substances 0.000 description 1
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- 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
Abstract
This utility model relates to a kind of MTP device, reaction gas after over-quenching passes through compressor boost, carry out washing compression three sections, alkali cleaning processes, the gas phase compressing four sections of outlets goes to depropanizing tower, liquid phase goes to debutanizing tower, the aqueous phase of each section of intersegmental knockout drum of compressor returns chilling tower, and hydrocarbon phase is sent to four sections of outlet knockout drums of compressor after supercharging；Debutanizing tower ejects material and goes to depropanizing tower, and tower reactor discharging enters dehexanizer；Dethanizer compressor is set between dethanizer and oil-absorption tower, oil-absorption tower uses recycled propane or C4 as lyosoption, tower top obtains the fuel gas without C2, and tower reactor discharging goes Analytic Tower to reclaim propane or C4 solvent, and Analytic Tower ejects material and goes to ethylene rectifying column acquisition ethylene side product.This utility model can effectively optimization technological process, reduce system energy consumption, reduce corrosive pipeline, reduce cost of investment.
Description
Technical field
This utility model relates to the field such as Coal Chemical Industry, gas chemical industry, is specifically related to a kind of MTP device.
Background technology
Propylene is one of most important basic organic, mainly for the production of chemical products such as polypropylene, acrylonitrile, expoxy propane, isopropylbenzene, octyl alconyl.Along with the economic sustained and rapid development of China, China is to the demand of propylene and downstream product thereof in significantly ascendant trend, and the problem of propylene shortage becomes increasingly conspicuous.Propylene is essentially from preparing ethylene by steam cracking device and catalytic cracking unit at present.In the case of oil supply day is becoming tight, it is developed the technological process being particularly waste propylene with methanol with oxide.
MTP process for preparing propylene from methanol refers to that the methanol synthesized with coal base or natural gas base, as raw material, by catalytic synthesis, produces the chemical process technology of propylene.MTP technique provides a kind of the raw material (natural gas or coal) with low-cost advantage and is converted into the approach of high added value propylene product.
Germany's Lu Qi Lurqi company's late 1990s successfully develops MTP technique.MTP technology is that methanol first changes into the mixture of dimethyl ether, unreacted methanol and water, then the proprietary ZSM-5 molecular sieve that Germany's south chemistry provides is used, under 450～500 DEG C of reaction conditions, make mixture mix with steam and be further converted into principal product propylene, obtain by-product gasoline, liquefied petroleum gas (LPG) and fuel gas etc. simultaneously.Produce the polymerization-grade propylene that impurity content is extremely low, and the high-knock rating gasoline of by-product is low containing benzene, not sulfur-bearing.
The most industrialized peaceful coal MTP device and the MTP technique of Datang MTP device equal equipment Imported From German EMH Company Lurgi, reaction gas uses deep cooling separating method.In addition to complicated refrigerant condenser system, in addition it is also necessary to the ice chest equipment of precise structure so that cryogenic separation flow process is complicated, investment is big.Demethanizer column overhead temperature is high, causes carrying by-product ethylene product in fuel gas secretly.After caustic wash tower is arranged on dethanizer, cause front system equipment, corrosive pipeline serious.Additionally, liquefied gas product purity is the highest, containing impurity such as DME, be unfavorable for the deep processing of liquefied gas.Above unfavorable factor, limits the development of MTP technique.
Chinese patent CN102304009A uses the rear separation process of conventional ethylene cracker, after caustic wash tower is arranged on compression two-stage nitration, and the problem solving front system equipment, corrosive pipeline, but need also exist for arranging the cryogenic system of complexity.
Utility model content
This utility model provides a kind of MTP device, in order to overcome at least one problem present in prior art.
For reaching above-mentioned purpose, this utility model provides a kind of MTP device, including: pre-chilling tower, chilling tower, process water stripper, process steam tower, methanol distillation column, hydrocarbon compressor, water scrubber charging knockout drum, water scrubber, caustic wash tower, depropanizing tower, gaseous hydrocarbon exsiccator, dethanizer, dethanizer suction port of compressor surge tank, dethanizer compressor, dethanizer compressor outlet knockout drum, oil-absorption tower, oil-absorption tower top condenser, oil-absorption tower charge air cooler, Analytic Tower, ethylene column, oxide extraction tower, DME removing tower, debutanizing tower, dehexanizer and propylene tower, wherein:
Pre-chilling tower is connected between MTP reactor and chilling tower, MTP reactor reacting gas out be introduced into the washing of pre-chilling tower chilled water (chw), and temperature enters chilling tower after reducing, and delivers to hydrocarbon compressor further and be compressed after cooling；The some processes water that pre-chilling tower bottom obtains through heat recovery rear portion for supplementing the fresh water (FW) of chilling tower top, another part is back to pre-chilling tower, remainder fresh water (FW) delivers to methanol distillation column, the fresh water (FW) part obtained at the bottom of chilling tower is returned chilling tower after cooling, another part enters process steam tower after coacervation, stripping, ion exchange purified treatment and produces steam, and the steam of generation returns MTP reactor；
After one section of import knockout drum of compressor, hydrocarbon compressor is entered from chilling top of tower gas hydrocarbon out, hydrocarbon compressor totally four sections, one section outlet knockout drum is entered after the cooling of one section outlet gas hydrocarbon, in one section outlet knockout drum, gas hydrocarbon removes compressor two-stage nitration, knockout drum lower liquid phase is divided into upper and lower two-layer, delivering to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, lower floor's aqueous phase returns one section of import knockout drum, finally returns to chilling tower；Entering second stage exit knockout drum after the cooling of second stage exit gas hydrocarbon, knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column；Entering three sections of outlet knockout drums after three sections of hydrocarbon coolings of working off one's feeling vent one's spleen, knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column；Top gas first removes alcohols organic oxygen compound through water scrubber wash cooling, then removes CO through caustic wash tower2, organic acid sour gas, subsequently into compressor four sections；Water at the bottom of water scrubber delivers to methanol distillation column, reclaims methanol therein and dimethyl ether returns MTP reactor and re-uses；Fresh water (FW) at the bottom of methanol distillation column tower, is largely recycled to water scrubber after cooling as detergent, and remaining send sewage disposal system as technique waste water；
The liquid hydrocarbon that hydrocarbon compressor is each section is collected to four sections of outlet knockout drums of compressor, and the liquid phase part of four sections of outlet knockout drums of compressor delivers to debutanizing tower after low-pressure steam heats, and gas phase portion goes to depropanizing tower；
Debutanizing tower tower top obtains carbon four component, delivers to depropanizing tower, and the carbon five obtained at the bottom of tower and above component are delivered to dehexanizing column and processed further；
Dehexanizer tower top discharging returns MTP reactor as circulation C5/C6, and dehexanizer tower reactor discharging is gasoline；
Depropanizing tower tower top discharging goes to gaseous hydrocarbon exsiccator after propylene refrigerant cools down, and goes to dethanizer after drying, and extraction tower is gone to aoxidize in depropanizing tower tower reactor output section, and part is recycled back into reactor as C4；
Dethanizer suction port of compressor surge tank is set between deethanization tower top and dethanizer compressor；Dethanizer ejects expects after dethanizer compressor boost, delivers to dethanizer compressor outlet knockout drum after cooling down with C3 cryogen；The gas phase methane hydrogen of dethanizer compressor outlet knockout drum tank deck enters oil-absorption tower, and tank bottoms liquid phase C2 part returns MTP reactor as cycle stock, and remainder enters oil-absorption tower；Propylene tower is gone in dethanizer tower reactor discharging；
DME removing tower is gone in oxidation extraction tower tower top discharging, and oxidation extraction tower tower reactor aqueous phase is back to methanol distillation column；
Propylene tower tower top obtains polymerization-grade propylene product, and the lyosoption on propane small part makeup oil absorption tower at the bottom of propylene tower tower, remainder is sent to battery limit (BL)；
Oil-absorption tower tower top arranges oil-absorption tower condenser, and Analytic Tower is gone in oil-absorption tower tower reactor discharging, and Analytic Tower tower reactor discharging is the recycled propane for solvent absorption, and ethylene column is gone in the discharging of tower top.
Further, the operation pressure of debutanizing tower is 2.15～2.55MPa, the operation pressure of dehexanizer is 0.20～0.60MPa, depropanizing tower operation pressure is 2.00～2.40MPa, propylene tower operation pressure is 2.00～2.40MPa, and the operation pressure of Analytic Tower is 1.85～2.25MPa, and oil-absorption tower operation pressure is 2.7～3.1Mpa, oxide extraction tower operation pressure is 2.00～2.4MPa, and DME removing tower operation pressure is 0.65～1.05MPa.
Further, DME removing tower top gaseous phase circulating water condensing, make reboiler thermal source with chilled water (chw) at the bottom of DME removing tower tower；Propylene tower top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of propylene tower tower.
Further, oil-absorption tower condenser uses and is not less than the propylene of-60 DEG C as cryogen, and oil-absorption tower arranges stage casing backflow, extracts one logistics in the middle part of oil-absorption tower out, returns oil-absorption tower through propylene refrigerant condensation after being not less than-50 DEG C.
Further, oil-absorption tower uses recycled propane or C4 to make lyosoption.
Novel separating technology for MTP device of the present utility model, there is no deep cooling ice chest, domethanizing column and ethylene compression refrigeration compressor, only use propylene refrigerant, lyosoption wherein used is all material in system, without extra outsourcing absorbent, and owing to MTP device ethylene side product content is relatively low, the lyosoption needed for therefore oil absorbs is the most less, saves plant investment and operating cost.In MTP device, within in existing running gear, in demethanizer column overhead fuel gas, ethylene contents is 8wt%, in this utility model, in oil-absorption tower tower top fuel gas, the content of ethylene is less than 0.7wt%, use technique of the present utility model to decrease the loss of ethylene product in fuel gas, improve economic benefit.
Novel separating technology for MTP device of the present utility model, the chilled water (chw) of pre-chilling tower and chilling tower is acted upon respectively, it is possible not only to more reasonably reclaim the waste heat of chilled water (chw), and the problem of cavitation above-mentioned two bursts of chilled water (chw) mixed processing brought in prior art can be avoided.Compress the entrance compression four sections after washing and alkali cleaning of three sections of gas hydrocarbon obtained can reduce downstream line, equipment corrosion.It is provided with oxide extraction tower and DME removing tower, it is ensured that oxide-free in C4 product, in order to the comprehensive utilization of C4.
Accompanying drawing explanation
In order to be illustrated more clearly that this utility model embodiment or technical scheme of the prior art, the accompanying drawing used required in embodiment or description of the prior art will be briefly described below, apparently, accompanying drawing in describing below is only embodiments more of the present utility model, for those of ordinary skill in the art, on the premise of not paying creative work, it is also possible to obtain other accompanying drawing according to these accompanying drawings.
Fig. 1 is that propane is as absorbent, the separating technology schematic flow sheet of the MTP reaction gas arranging the backflow of oil-absorption tower stage casing and C4 purification；
Fig. 2 is that C4 is as absorbent, the separating technology schematic flow sheet of the MTP reaction gas being not provided with oil absorption stage casing backflow and C4 purification.
Accompanying drawing 1 description of symbols: 1-pre-chilling tower；2-chilling tower；3-process water stripper；4-process steam tower；5-one section of suction tank of methanol distillation column 6-compressor；7-compressor one section；8-compressor two-stage nitration suction tank；9-compressor two-stage nitration；Three sections of suction tanks of 10-compressor；11-compressor three sections；12-water scrubber charging knockout drum；13-water scrubber；14-caustic wash tower；15-compressor four sections；Four sections of outlet knockout drums of 16-compressor；17-depropanizing tower；18-gaseous hydrocarbon exsiccator；19-dethanizer；20-dethanizer suction port of compressor surge tank；21-dethanizer compressor；22-dethanizer compressor outlet knockout drum；23-oil-absorption tower；24-oil-absorption tower top condenser；25-oil-absorption tower charge air cooler；26-Analytic Tower；27-ethylene column；28-oxide extraction tower；29-DME removing tower；30-debutanizing tower；31-dehexanizer；32-propylene tower；33-dehexanizer；32-propylene tower；34-coacervation device；35-ion exchanger；A-MTP reactor product；B-reaction vapor；C-fuel gas；D-ethylene product；E-ethane；F-fixed gas；G-DME guard bed；H-propylene product；I-propane；J-gasoline products；K-gasoline stabilizer；L-C4 product；M-C5/C6 circulates；N-C4 circulates；O-C2 circulates；P-technique waste water；Q-recycle methanol；R-methanol；S-propane supplements；T-DME dereaction district.
Detailed description of the invention
Below in conjunction with the accompanying drawing in this utility model embodiment, the technical scheme in this utility model embodiment is clearly and completely described, it is clear that described embodiment is only a part of embodiment of this utility model rather than whole embodiments.Based on the embodiment in this utility model, the every other embodiment that those of ordinary skill in the art are obtained under not paying creative work premise, broadly fall into the scope of this utility model protection.
Fig. 1 is that propane is as absorbent, the separating technology schematic flow sheet of the MTP reaction gas arranging the backflow of oil-absorption tower stage casing and C4 purification；Below in conjunction with Fig. 1, embodiment 1 of the present utility model is described in detail.
As it is shown in figure 1, the reacting gas about 190 DEG C drawn from MTP reactor, being introduced into the washing of pre-chilling tower chilled water (chw), temperature enters chilling tower after being down to about 50 DEG C, is cooled to about 40 DEG C, is then sent to compression unit and is compressed.The some processes water obtained at the bottom of pre-chilling tower through heat recovery rear portion for supplementing the fresh water (FW) of chilling tower top, another part is back to pre-chilling tower, remaining fresh water (FW) delivers to methanol distillation column, the fresh water (FW) part obtained at the bottom of chilling tower is returned chilling tower after cooling, another part enters process steam tower after coacervation, stripping, ion exchange purified treatment and produces steam, and the steam of generation returns MTP reactor.
After one section of import knockout drum of compressor, hydrocarbon compressor is entered from chilling top of tower gas hydrocarbon out, hydrocarbon compressor totally four sections, one section outlet gas hydrocarbon enters one section outlet knockout drum after being cooled to about 50 DEG C, in one section outlet knockout drum, gas hydrocarbon removes compressor two-stage nitration, knockout drum lower liquid phase is divided into upper and lower two-layer, delivering to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, lower floor's aqueous phase returns one section of import knockout drum, finally returns to chilling tower.Second stage exit gas hydrocarbon enters second stage exit knockout drum after being cooled to about 50 DEG C, and knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column.Three sections of hydrocarbon of working off one's feeling vent one's spleen enter three sections of outlet knockout drums after being cooled to about 50 DEG C, and knockout drum lower liquid phase divides upper and lower two-layer, deliver to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column.Top gas is first through organic oxygen compounds such as water scrubber wash cooling to about 40 DEG C removing alcohols, then removes CO through caustic wash tower2, the sour gas such as organic acid, subsequently into compressor four sections.Water at the bottom of water scrubber delivers to methanol distillation column, reclaims methanol therein and dimethyl ether (DME) returns MTP reactor and is again used.Fresh water (FW) at the bottom of methanol distillation column tower, is largely recycled to water scrubber after cooling as detergent, and remaining send sewage disposal system as technique waste water.
The liquid hydrocarbon compressing each section is collected to four sections of outlet knockout drums of compressor, and the liquid phase part of this tank delivers to debutanizing tower after low-pressure steam heats, and gas phase portion goes to depropanizing tower.
Debutanizing tower tower top obtains carbon four component, delivers to depropanizing tower, and tower bottom product is mainly carbon five and above component, delivers to dehexanizing column and processes further, and debutanizing tower operation pressure is 2.35MPa.
Dehexanizer tower top discharging returns MTP reactor as circulation C5/C6, and tower reactor discharging is gasoline by-product, and dehexanizer operation pressure is 0.40MPa.
Depropanizing tower tower top discharging goes to gaseous hydrocarbon exsiccator after propylene refrigerant cools down, and goes to dethanizer after drying, and extraction tower is gone to aoxidize in tower reactor output section, and part is recycled back into reactor as C4.Depropanizing tower uses conventional rectification, owing to the catalyst of MTP reactor reduces at last stage reaction conversion ratio, and DME content overproof, therefore introduce methanol at last stage reaction and remove tower top DME as lyosoption.Depropanizing tower operation pressure is 2.20MPa.
Arranging dethanizer suction port of compressor surge tank between deethanization tower top and dethanizer compressor, the purpose of this tank is keep the even running of dethanizer compressor and do not allow droplet entrainment enter compressor.Tower top discharging, after dethanizer compressor boost to 3.1Mpa, delivers to dethanizer compressor outlet knockout drum after sending-37 DEG C with the cooling of C3 cryogen.The gas phase methane hydrogen of knockout drum tank deck enters oil-absorption tower, and the liquid phase C2 part of separation tank bottom returns MTP reactor as cycle stock, and remainder enters oil-absorption tower.Propylene tower is gone in dethanizer tower reactor discharging.
DME removing tower is gone in oxidation extraction tower tower top discharging, and tower reactor aqueous phase is back to methanol distillation column.DME removing tower is conventional rectification, top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of tower.
Propylene tower tower top obtains polymerization-grade propylene product, and purity is 99.6wt%, propane small part makeup oil absorption tower lyosoption at the bottom of tower, remainder is sent to battery limit (BL), propylene tower operation pressure is 2.20MPa, and top gaseous phase circulating water condensing makees reboiler thermal source with chilled water (chw) at the bottom of tower.
Oil-absorption tower uses recycled propane or C4 to make lyosoption, and tower top arranges oil-absorption tower condenser, uses the propylene of-41 DEG C as cryogen.Stage casing backflow is additionally set, in the middle part of oil-absorption tower, extracts one logistics out, after-41 DEG C of propylene refrigerant condensations are to-37 DEG C, return oil-absorption tower.Oil-absorption tower operation pressure is 2.9Mpa, and in tower top fuel gas, the content of ethylene controls within 0.6wt%.Analytic Tower is gone in oil-absorption tower tower reactor discharging, and Analytic Tower tower reactor discharging is the recycled propane for solvent absorption, and ethylene column is gone in the discharging of tower top.Analytic Tower operation pressure is 2.05MPa.
Ethylene column tower top obtains polymer grade ethylene product, and purity is 99.95wt%, and tower reactor obtains ethane.Ethylene column operation pressure is 1.8MPa, and top gaseous phase propylene refrigerant condenses, and makees reboiler thermal source with propylene refrigerant at the bottom of tower.
Fig. 2 is that C4 is as absorbent, the separating technology schematic flow sheet of the MTP reaction gas being not provided with oil absorption stage casing backflow and C4 purification.Below in conjunction with Fig. 2, embodiment 2 of the present utility model is described in detail.
As in figure 2 it is shown, the reacting gas about 190 DEG C drawn from MTP reactor, being introduced into the washing of pre-chilling tower chilled water (chw), temperature enters chilling tower after being down to about 50 DEG C, is cooled to about 40 DEG C, is then sent to compression unit and is compressed.The some processes water obtained at the bottom of pre-chilling tower through heat recovery rear portion for supplementing the fresh water (FW) of chilling tower top, another part is back to pre-chilling tower, remaining fresh water (FW) delivers to methanol distillation column, the fresh water (FW) part obtained at the bottom of chilling tower is returned chilling tower after cooling, another part enters process steam tower after coacervation, stripping, ion exchange purified treatment and produces steam, and the steam of generation returns MTP reactor.
After one section of import knockout drum of compressor, hydrocarbon compressor is entered from chilling top of tower gas hydrocarbon out, hydrocarbon compressor totally four sections, one section outlet gas hydrocarbon enters one section outlet knockout drum after being cooled to about 50 DEG C, in one section outlet knockout drum, gas hydrocarbon removes compressor two-stage nitration, knockout drum lower liquid phase is divided into upper and lower two-layer, delivering to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, lower floor's aqueous phase returns one section of import knockout drum, finally returns to chilling tower.Second stage exit gas hydrocarbon enters second stage exit knockout drum after being cooled to about 50 DEG C, and knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column.Three sections of hydrocarbon of working off one's feeling vent one's spleen enter three sections of outlet knockout drums after being cooled to about 50 DEG C, and knockout drum lower liquid phase divides upper and lower two-layer, deliver to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column.Top gas is first through organic oxygen compounds such as water scrubber wash cooling to about 40 DEG C removing alcohols, then removes CO through caustic wash tower2、H2The sour gas such as S, subsequently into compressor four sections.Water at the bottom of water scrubber delivers to methanol distillation column, reclaims methanol therein and dimethyl ether (DME) returns MTP reactor and is again used.Fresh water (FW) at the bottom of methanol distillation column tower, is largely recycled to water scrubber after cooling as detergent, and remaining send sewage disposal system as technique waste water.
The liquid hydrocarbon compressing each section is collected to four sections of outlet knockout drums of compressor, and the liquid phase part of this tank delivers to debutanizing tower after low-pressure steam heats, and gas phase portion goes to depropanizing tower.
Debutanizing tower tower top obtains carbon four component, delivers to depropanizing tower, and tower bottom product is mainly carbon five and above component, delivers to dehexanizing column and processes further, and debutanizing tower operation pressure is 2.35MPa.
Dehexanizer tower top discharging returns MTP reactor as circulation C5/C6, and tower reactor discharging is gasoline by-product, and dehexanizer operation pressure is 0.40MPa.
Depropanizing tower tower top discharging goes to gaseous hydrocarbon exsiccator after propylene refrigerant cools down, and goes to dethanizer after drying, and tower reactor output section is recycled back into reactor as C4, and remainder is sent to battery limit (BL) as C4 product.Depropanizing tower operation pressure is 2.20MPa.
Arranging dethanizer suction port of compressor surge tank between deethanization tower top and dethanizer compressor, the purpose of this tank is keep the even running of dethanizer compressor and do not allow droplet entrainment enter compressor.Tower top discharging, after dethanizer compressor boost to 3.1Mpa, delivers to dethanizer compressor outlet knockout drum after sending-37 DEG C with the cooling of C3 cryogen.The gas phase methane hydrogen of knockout drum tank deck enters oil-absorption tower, and the liquid phase C2 part of separation tank bottom returns MTP reactor as cycle stock, and remainder enters oil-absorption tower.Propylene tower is gone in dethanizer tower reactor discharging.
Removing DME in propylene tower, tower top obtains polymerization-grade propylene product, and purity is 99.6wt%, propane small part makeup oil absorption tower lyosoption at the bottom of tower, remainder is sent to battery limit (BL), and propylene tower operation pressure is 2.20MPa, top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of tower.
Oil-absorption tower uses C4 lyosoption, and tower top arranges oil-absorption tower condenser, uses the propylene of-41 DEG C as cryogen.Oil-absorption tower operation pressure is 2.9Mpa, and in tower top fuel gas, the content of ethylene controls within 0.7wt%.Analytic Tower is gone in oil-absorption tower tower reactor discharging, and Analytic Tower tower reactor discharging is the C4 for solvent absorption, and ethylene column is gone in the discharging of tower top.Analytic Tower operation pressure is 2.05MPa.
Ethylene column tower top obtains polymer grade ethylene product, and purity is 99.95wt%, and tower reactor obtains ethane.Ethylene column operation pressure is 1.8MPa, and top gaseous phase propylene refrigerant condenses, and makees reboiler thermal source with propylene refrigerant at the bottom of tower.
Compared with prior art, energy consumption of the present utility model is low, small investment, material recovery rate are high and simple to operate reliable.
Being below the novel separating technology embodiment for MTP device of the present utility model, this technique comprises the following steps:
(1) MTP reaction gas passes through pre-chilling tower and chilling tower chilling, the fresh water (FW) of pre-chilling tower and chilling tower is acted upon respectively, the some processes water obtained at the bottom of pre-chilling tower through heat recovery rear portion for supplementing the fresh water (FW) of chilling tower top, another part is back to pre-chilling tower, remaining fresh water (FW) delivers to methanol distillation column, the fresh water (FW) part obtained at the bottom of chilling tower returns chilling tower after cooling, entering process steam tower after the purified process of another part and produce steam, the steam of generation returns MTP reactor.
(2) reaction gas after chilling passes through compressor boost, carry out washing compression three sections, alkali cleaning processes, the gas phase compressing four sections of outlets goes to depropanizing tower, liquid phase goes to debutanizing tower, the aqueous phase of each section of intersegmental knockout drum of compressor returns chilling tower, and hydrocarbon phase is sent to four sections of outlet knockout drums of compressor after supercharging.
(3) debutanizing tower ejects material and goes to depropanizing tower, and tower reactor discharging enters dehexanizer.Dehexanizer tower top discharging returns MTP reactor as circulation C5/C6, and tower reactor discharging is gasoline by-product.Depropanizing tower tower top discharging is through going to dethanizer after drying, and tower reactor C4 component Parts obtains qualified C4 product as recycle stock Returning reactor, remainder through purification processes.Dethanizer ejects material and enters dethanizer compressor outlet knockout drum, whole gas phases and Partial Liquid Phase C2 entrance oil-absorption tower after supercharging cools down, and remaining liquid phase C2 is done cycle stock and returned MTP reactor.Propylene tower is gone in deethanization tower reactor discharging, and propylene tower tower top discharging obtains polymerization-grade propylene product through product protection bed.
(4) using recycled propane or C4 to obtain the fuel gas without ethylene as lyosoption, tower top in oil-absorption tower, tower reactor discharging goes Analytic Tower to reclaim propane or C4 solvent, and Analytic Tower ejects material and goes to ethylene rectifying column acquisition ethylene side product.
Purified treatment described in step (1) includes coacervation, stripping and the step of ion exchange.
Water scrubber described in step (2), caustic wash tower operation pressure limit is 0.85～1.25MPa, preferably 1.05MPa.
Purification processes described in step (3) refers to depropanizing tower tower reactor part C4 through peroxide extraction tower, removes the DME come from upstream and methanol that depropanizing tower teeming enters.DME removing tower is gone in oxidation extraction tower tower top discharging, ensures that C4 product is without DME through rectification.When DME content is relatively low in depropanizing tower, purification processes can not be set.The operation pressure limit 2.00～2.40Mpa of oxide extraction tower, preferably 2.20Mpa.The operation pressure limit 0.65～1.05Mpa of DME removing tower, preferably 0.85Mpa.
The operation pressure limit of depropanizing tower described in step (3) is 2.00MPa～2.40MPa, preferably 2.20MPa.Described depropanizing tower uses conventional rectification, when DME content is higher, can introduce methanol and remove tower top DME as lyosoption.
Dethanizer described in step (3), tower top enters the gas hydrocarbon propylene refrigerant of oil-absorption tower and condenses, and makees reboiler thermal source with chilled water (chw) at the bottom of tower, and dethanizer operation pressure limit is 1.65～2.05MPa, preferably 1.85MPa.
Debutanizing tower described in step (3), tower operation pressure limit is 2.15～2.55MPa, preferably 2.35MPa.
Dehexanizer described in step (3), tower operation pressure limit is 0.20～0.60MPa, preferably 0.40MPa.
Propylene tower described in step (3); tower top obtains polymerization-grade propylene through product protection bed removing DME, and described propylene tower operation pressure limit is 2.00～2.40MPa, preferably 2.20MPa; top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of tower.
Oil-absorption tower described in step (4), can not set oil-absorption tower charge air cooler by conventional distillation Deethanizer design, it is also possible to arrange charge air cooler to reduce energy consumption.Oil-absorption tower operation pressure limit is 2.7～3.1MPa, preferably 2.9MPa, oil-absorption tower top condenser uses and is not less than-60 DEG C of cryogens as cooling medium, preferably-41 DEG C propylene refrigerants, tower top lyosoption uses and is not less than the propane of-60 DEG C or C4 as overhead reflux, preferably-41 DEG C propane or C4, in tower, condenser extraction is not less than the mixed material of-60 DEG C as stage casing backflow, preferably-37 DEG C mixed materials.In oil-absorption tower tower top fuel gas, the content of ethylene is less than 0.7wt%.
Analytic Tower described in step (4), tower operation pressure limit is 1.85～2.25MPa, and preferably 2.05MPa, owing to oil-absorption tower top can carry a small amount of lyosoption secretly, it is therefore desirable to supplement lyosoption in device.
Ethylene rectifying column described in step (4), pressure tower scope is 1.55～1.95MPa, preferably 1.75MPa.Top gaseous phase propylene refrigerant condenses, and makees reboiler thermal source with propylene refrigerant at the bottom of tower.
Novel separating technology for MTP device of the present utility model, there is no deep cooling ice chest, domethanizing column and ethylene compression refrigeration compressor, only use propylene refrigerant, lyosoption wherein used is all material in system, without extra outsourcing absorbent, and owing to MTP device ethylene side product content is relatively low, the lyosoption needed for therefore oil absorbs is the most less, saves plant investment and operating cost.In MTP device, within in existing running gear, in demethanizer column overhead fuel gas, ethylene contents is 8wt%, in this utility model, in oil-absorption tower tower top fuel gas, the content of ethylene is less than 0.7wt%, use technique of the present utility model to decrease the loss of ethylene product in fuel gas, improve economic benefit.
Novel separating technology for MTP device of the present utility model, the chilled water (chw) of pre-chilling tower and chilling tower is acted upon respectively, it is possible not only to more reasonably reclaim the waste heat of chilled water (chw), and the problem of cavitation above-mentioned two bursts of chilled water (chw) mixed processing brought in prior art can be avoided.Compress the entrance compression four sections after washing and alkali cleaning of three sections of gas hydrocarbon obtained can reduce downstream line, equipment corrosion.It is provided with oxide extraction tower and DME removing tower, it is ensured that oxide-free in C4 product, in order to the comprehensive utilization of C4.
One of ordinary skill in the art will appreciate that: accompanying drawing is the schematic diagram of an embodiment, module or flow process in accompanying drawing are not necessarily implemented necessary to this utility model.
One of ordinary skill in the art will appreciate that: the module in device in embodiment can describe in the device being distributed in embodiment according to embodiment, it is also possible to carries out respective change and is disposed other than in one or more devices of the present embodiment.The module of above-described embodiment can merge into a module, it is also possible to is further split into multiple submodule.
Last it is noted that above example is only in order to illustrate the technical solution of the utility model, it is not intended to limit；Although this utility model being described in detail with reference to previous embodiment, it will be understood by those within the art that: the technical scheme described in previous embodiment still can be modified by it, or wherein portion of techniques feature is carried out equivalent；And these amendments or replacement, do not make the essence of appropriate technical solution depart from the spirit and scope of this utility model embodiment technical scheme.
Claims (5)
1. a MTP device, it is characterized in that, including: pre-chilling tower, chilling tower, process water stripper, process steam tower, methanol distillation column, hydrocarbon compressor, water scrubber charging knockout drum, water scrubber, caustic wash tower, depropanizing tower, gaseous hydrocarbon exsiccator, dethanizer, dethanizer suction port of compressor surge tank, dethanizer compressor, dethanizer compressor outlet knockout drum, oil-absorption tower, oil-absorption tower top condenser, oil-absorption tower charge air cooler, Analytic Tower, ethylene column, oxide extraction tower, DME removing tower, debutanizing tower, dehexanizer and propylene tower, wherein:
Pre-chilling tower is connected between MTP reactor and chilling tower, MTP reactor reacting gas out be introduced into the washing of pre-chilling tower chilled water (chw), and temperature enters chilling tower after reducing, and delivers to hydrocarbon compressor further and be compressed after cooling；The some processes water that pre-chilling tower bottom obtains through heat recovery rear portion for supplementing the fresh water (FW) of chilling tower top, another part is back to pre-chilling tower, remainder fresh water (FW) delivers to methanol distillation column, the fresh water (FW) part obtained at the bottom of chilling tower is returned chilling tower after cooling, another part enters process steam tower after coacervation, stripping, ion exchange purified treatment and produces steam, and the steam of generation returns MTP reactor；
After one section of import knockout drum of compressor, hydrocarbon compressor is entered from chilling top of tower gas hydrocarbon out, hydrocarbon compressor totally four sections, one section outlet knockout drum is entered after the cooling of one section outlet gas hydrocarbon, in one section outlet knockout drum, gas hydrocarbon removes compressor two-stage nitration, knockout drum lower liquid phase is divided into upper and lower two-layer, delivering to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, lower floor's aqueous phase returns one section of import knockout drum, finally returns to chilling tower；Entering second stage exit knockout drum after the cooling of second stage exit gas hydrocarbon, knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column；Entering three sections of outlet knockout drums after three sections of hydrocarbon coolings of working off one's feeling vent one's spleen, knockout drum lower liquid phase divides upper and lower two-layer, delivers to four sections of outlet knockout drums of hydrocarbon compressor after the liquid hydrocarbon supercharging of upper strata, and lower floor's aqueous phase returns quenching water column；Top gas first removes alcohols organic oxygen compound through water scrubber wash cooling, then removes CO through caustic wash tower2, organic acid sour gas, subsequently into compressor four sections；Water at the bottom of water scrubber delivers to methanol distillation column, reclaims methanol therein and dimethyl ether returns MTP reactor and re-uses；Fresh water (FW) at the bottom of methanol distillation column tower, is largely recycled to water scrubber after cooling as detergent, and remaining send sewage disposal system as technique waste water；
The liquid hydrocarbon that hydrocarbon compressor is each section is collected to four sections of outlet knockout drums of compressor, and the liquid phase part of four sections of outlet knockout drums of compressor delivers to debutanizing tower after low-pressure steam heats, and gas phase portion goes to depropanizing tower；
Debutanizing tower tower top obtains carbon four component, delivers to depropanizing tower, and the carbon five obtained at the bottom of tower and above component are delivered to dehexanizing column and processed further；
Dehexanizer tower top discharging returns MTP reactor as circulation C5/C6, and dehexanizer tower reactor discharging is gasoline；
Depropanizing tower tower top discharging goes to gaseous hydrocarbon exsiccator after propylene refrigerant cools down, and goes to dethanizer after drying, and depropanizing tower tower reactor output section is gone to aoxidize extraction tower, and remainder is recycled back into reactor as C4；
Dethanizer suction port of compressor surge tank is set between deethanization tower top and dethanizer compressor；Dethanizer ejects expects after dethanizer compressor boost, delivers to dethanizer compressor outlet knockout drum after cooling down with C3 cryogen；The gas phase methane hydrogen of dethanizer compressor outlet knockout drum tank deck enters oil-absorption tower, and tank bottoms liquid phase C2 part returns MTP reactor as cycle stock, and remainder enters oil-absorption tower；Propylene tower is gone in dethanizer tower reactor discharging；
DME removing tower is gone in oxidation extraction tower tower top discharging, and oxidation extraction tower tower reactor aqueous phase is back to methanol distillation column；
Propylene tower tower top obtains polymerization-grade propylene product, and the lyosoption on propane small part makeup oil absorption tower at the bottom of propylene tower tower, remainder is sent to battery limit (BL)；
Oil-absorption tower tower top arranges oil-absorption tower condenser, and Analytic Tower is gone in oil-absorption tower tower reactor discharging, and Analytic Tower tower reactor discharging is the recycled propane for solvent absorption, and ethylene column is gone in the discharging of tower top.
MTP device the most according to claim 1, it is characterized in that, the operation pressure of debutanizing tower is 2.15～2.55MPa, the operation pressure of dehexanizer is 0.20～0.60MPa, depropanizing tower operation pressure is 2.00～2.40MPa, propylene tower operation pressure is 2.00～2.40MPa, the operation pressure of Analytic Tower is 1.85～2.25MPa, oil-absorption tower operation pressure is 2.7～3.1Mpa, oxide extraction tower operation pressure is 2.00～2.4MPa, and DME removing tower operation pressure is 0.65～1.05MPa.
MTP device the most according to claim 1, it is characterised in that DME removing tower top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of DME removing tower tower；Propylene tower top gaseous phase circulating water condensing, makees reboiler thermal source with chilled water (chw) at the bottom of propylene tower tower.
MTP device the most according to claim 1, it is characterized in that, oil-absorption tower condenser uses and is not less than the propylene of-60 DEG C as cryogen, and oil-absorption tower arranges stage casing backflow, extract one logistics in the middle part of oil-absorption tower out, after being not less than-50 DEG C, return oil-absorption tower through propylene refrigerant condensation.
MTP device the most according to claim 1, it is characterised in that oil-absorption tower uses recycled propane or C4 to make lyosoption.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105503492A (en) * | 2015-12-30 | 2016-04-20 | 中国寰球工程公司 | MTP (methanol to propylene) device and novel separation process thereof |
| CN111394116A (en) * | 2019-08-12 | 2020-07-10 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105503492A (en) * | 2015-12-30 | 2016-04-20 | 中国寰球工程公司 | MTP (methanol to propylene) device and novel separation process thereof |
| CN111394116A (en) * | 2019-08-12 | 2020-07-10 | 中国石化工程建设有限公司 | Oil gas recovery method and device |
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Address after: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee after: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. Address before: Two road 100012 Beijing city Chaoyang District high tech Industrial Park, No. 1. Patentee before: China Huanqiu Contracting & Engineering Corp. |
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