CN108358739A - A kind of oil-water-gas separating system and method for process for preparing propylene from methanol - Google Patents
A kind of oil-water-gas separating system and method for process for preparing propylene from methanol Download PDFInfo
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- CN108358739A CN108358739A CN201810338561.0A CN201810338561A CN108358739A CN 108358739 A CN108358739 A CN 108358739A CN 201810338561 A CN201810338561 A CN 201810338561A CN 108358739 A CN108358739 A CN 108358739A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 510
- 238000000034 method Methods 0.000 title claims abstract description 300
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 51
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 471
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 282
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 277
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 273
- 230000008569 process Effects 0.000 claims abstract description 255
- 238000000926 separation method Methods 0.000 claims abstract description 126
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 36
- 238000011084 recovery Methods 0.000 claims abstract description 36
- 238000010790 dilution Methods 0.000 claims abstract description 30
- 239000012895 dilution Substances 0.000 claims abstract description 30
- 238000004821 distillation Methods 0.000 claims description 70
- 238000003809 water extraction Methods 0.000 claims description 64
- 239000007791 liquid phase Substances 0.000 claims description 26
- 239000000203 mixture Substances 0.000 claims description 25
- 239000010865 sewage Substances 0.000 claims description 23
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 21
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 21
- 239000004571 lime Substances 0.000 claims description 21
- 150000003839 salts Chemical class 0.000 claims description 20
- 239000011344 liquid material Substances 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 10
- 238000010992 reflux Methods 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 5
- 239000013618 particulate matter Substances 0.000 claims description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims 1
- 238000005406 washing Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 239000004519 grease Substances 0.000 abstract 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 80
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 80
- 239000007789 gas Substances 0.000 description 79
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- 238000001035 drying Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000010791 quenching Methods 0.000 description 5
- 159000000000 sodium salts Chemical class 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 230000000171 quenching effect Effects 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000010025 steaming Methods 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of grease gas separating system and method for process for preparing propylene from methanol, the grease gas separating system, including hydrocarbon water separative element, Oil-gas Separation unit, process steam production unit and methanol recovery unit；Hydrocarbon water separative element is for detaching the logistics of reaction product containing MTP and dilution steam generation；The water that Oil-gas Separation unit is used for entrained in the gaseous hydrocarbon and heavy hydrocarbon component separating obtained to hydrocarbon water separative element detaches；Process steam production unit is additionally operable to handle the water for having extracted hydrocarbon component to obtain process steam for being stripped the condensed water for being at least partially separate heavy hydrocarbon component；Methanol recovery unit is for handling the condensed water for being at least partially separate heavy hydrocarbon component, to isolate methanol contained therein, DME and light component fixed gas.MTP reaction products and reaction water and process steam, can more be totally separated from, ensure the long period even running of device by the piece-rate system of the present invention.
Description
Technical field
The present invention relates to the oil-water-gas isolation technics of process for preparing propylene from methanol products therefrom, more particularly to a kind of to be used for methanol
Oil-water-the gas separating system and method for propylene technique processed.
Background technology
Propylene is the most important basic organic for being only second to ethylene.With the expansion year by year of its derivative application field
Exhibition, demand are growing day by day.But since increasingly plaque is weary for petroleum resources, hence it is imperative that the propylene of development non-petroleum base prepares work
Skill.Currently, having been enter into large-scale production by raw material methanol of coal/natural gas, preparing light olefins from methanol (MTO/MTP) has original
The advantages that material derives from a wealth of sources, is at low cost, the national conditions for being suitble to China rich in coal and poor in oil.
Preparing propylene from methanol (MTP) technique is that under the effect of the catalyst, dimethyl ether/methanol mixture chemically reacts,
Generate the product mix containing unconverted methanol and hydrocarbon.Product is cooling, separation process be unreacted methanol Returning reactor with
The part that propylene is connected with ethylene distillation processing, that is, in product cooling, separation process, generated from MTP reactors
Product is cooled, so that gas, You Heshui are sufficiently separated.The cooling and separation of MTP reactor products are necessary, therefore are detached
Efficiency is most important.Rational piece-rate system can improve the efficiency of MTP technological designs, thus how design piece-rate system,
It is the important part of MTP technologies.
In October, 2010,500,000 tons/year of coal-based methanol systems third that Shenhua Ningxia Coal Industry Group is introduced from German Lurgi companies
Alkene (MTP) project puts into industrial production.So far, which ran more than 5 years.As most of industrialized for the first time large
Chemicals production technology is the same, and for Lurgi MTP techniques while highly selective production propylene, there is also many places to need to improve it
Place.In MTP device operational process, water-oil separating problem is always to perplex the bottleneck of device even running.Water-oil separating mainly relates to
And quenching column and pre- quenching column, oxide extraction tower and extraction tower, the water-oil separating problem of wherein quenching column and pre- quenching column are
Most merit attention.Oil-water separation is bad to would potentially result in Quench pump entrance band oil and gas erosion jump vehicle, and then leads to hydrocarbon pressure
Contracting machine inlet temperature is high and jumps the accidents such as vehicle.However, current chilling train technical flow design considers needs of production
Deficiency, it is bad for product separation system gas, oil and water separating effect.How more thoroughly and MTP is efficiently produced into work
Gas, You Heshui in skill are kept completely separate, and are that currently there is an urgent need for one of technological difficulties to make a breakthrough by those skilled in the art.
Invention content
In view of this, the present invention provides a kind of oil-water-gas separating system for process for preparing propylene from methanol, base is also provided
In oil-water-gas separation method for process for preparing propylene from methanol products therefrom of the piece-rate system.Segregative line using the present invention
MTP reaction products and reaction water and process steam, can more be totally separated from by system, ensure the long week of preparing propylene by coal-based methanol device
Phase even running, and the drying of the operation and hydrocarbon product conducive to subsequent gases compressibility.
The present invention is to reach its purpose, and the technical solution of use is as follows：
First aspect present invention provides a kind of oil-water-gas separating system for process for preparing propylene from methanol, including hydrocarbon-water
Separative element, oil-gas separative element, process steam production unit and methanol recovery unit；
The hydrocarbon-water separative element is for detaching the logistics of reaction product containing MTP and dilution steam generation, to obtain gas
State hydrocarbon, heavy hydrocarbon component and the condensed water for having detached heavy hydrocarbon component；
The oil-gas separative element is used for in the hydrocarbon-water separative element separating obtained gaseous hydrocarbon and heavy hydrocarbon component
The water of entrained with is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；
The process steam production unit is used for at least partly described separation separating obtained to the hydrocarbon-water separative element
The condensed water of heavy hydrocarbon component is stripped, to extract the water that hydrocarbon component therein and obtaining has extracted hydrocarbon component, also
For handling the water for having extracted hydrocarbon component to obtain the process steam for having detached the drop containing salt；
The methanol recovery unit is weighed at least partly described detached separating obtained to the hydrocarbon-water separative element
The condensed water of the hydrocarbon component is handled, to isolate methanol contained therein, DME and light component fixed gas.
In some preferred embodiments of the invention, the hydrocarbon-water separative element includes pre- chilling tower, chilling tower and chilled water (chw)
Knockout drum；
Wherein, the pre- chilling tower is equipped with the first entrance for inputting chilled water (chw) and lye, is additionally provided with and contains for inputting
The second entrance of the logistics of MTP reaction products and dilution steam generation, the first entrance is located above the second entrance, described pre-
Chilling tower is for contacting the logistics of the reaction product containing MTP and dilution steam generation with chilled water (chw) and lye, to contain MTP to described
The logistics of reaction product and dilution steam generation is cooled down and is washed, and gaseous stream, heavy hydrocarbon component and condensed water are obtained；
The chilling tower is equipped with the third entrance for inputting chilled water (chw) and lye, is additionally provided with for inputting from described pre-
4th entrance of the gaseous stream of chilling tower, the third entrance are located at the 4th entrance top, and the chilling tower is used for will
Gaseous stream from the pre- chilling tower is contacted with chilled water (chw) and lye, the gaseous stream is cooled down and be washed,
Obtain gaseous hydrocarbon, heavy hydrocarbon component and condensed water；
The chilling water separation tank is connected to the pre- chilling tower and the chilling tower by condensed water conveyance conduit respectively,
The chilling water separation tank is for receiving the condensed water conveyed by the condensed water conveyance conduit and to being remained in the condensed water
Heavy hydrocarbon component detached, with the condensed water for obtaining heavy hydrocarbon component He having detached heavy hydrocarbon component；
In some of the invention preferred embodiments, chilling water separation tank first entrance, the urgency with pre- chilling tower respectively
It is connected to by chilling water circulating pipe between the third entrance of cold tower, it is at least partly described for obtaining chilling water separation tank
The condensed water for having detached heavy hydrocarbon component is recycled to the pre- chilling tower and chilling tower as chilled water (chw) respectively.
In some preferred embodiments of the invention, the oil-gas separative element includes compressor buffer tank, compressor and oil
Gas knockout drum；
Wherein, it is connected to by gaseous hydrocarbon conveyance conduit between the compressor buffer tank and the chilling tower, the compression
Machine surge tank is for detaching the water carried secretly in the gaseous hydrocarbon from the chilling tower, to obtain liquid material and separation
The gaseous hydrocarbon of the water of entrainment；Preferably, liquid material conveyance conduit is also associated between the compressor buffer tank and chilling tower,
It is recycled to chilling tower with the liquid material for obtaining compressor buffer tank separation；
The compressor is connected to the compressor buffer tank, and the compressor is for receiving the compressor buffer tank point
The gaseous hydrocarbon of the water for having detached entrainment from gained, and it is compressed and is cooled down to obtain gas mixture；
The catch pot is connected to the compressor by gas mixture conveyance conduit, the catch pot with
The pre- chilling tower, chilling tower are connected to by heavy hydrocarbon component conveyance conduit respectively with chilling water separation tank, the catch pot
For to the gas mixture from the compressor and the heavy hydrocarbon from the pre- chilling tower, chilling tower and chilling water separation tank
The water carried secretly in component is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；Preferably, the catch pot
It is connected to by residual water conveyance conduit between compressor buffer tank, for the remaining water to be fed through compressor buffering
Tank.
In some preferred embodiments of the invention, the process steam production unit includes process water extraction tower, technique steaming
Vapour generator and process steam knockout drum；
Wherein, the process water extraction tower is connected to chilling water separation tank by the first chilled water (chw) conveyance conduit, and described
One chilled water (chw) conveyance conduit is used for at least partly described condensed water for having detached heavy hydrocarbon component obtained by chilling water separation tank is defeated
Enter to process water extraction tower；The process water extraction tower is equipped with the process steam input port for inputting process steam, the work
The condensed water and work for having detached heavy hydrocarbon component that skill water extraction tower is used to be inputted by the first chilled water (chw) conveyance conduit
Skill steam is contacted to extract remaining hydrocarbon component, and obtains the water for having extracted hydrocarbon component；Preferably, the process water is taken out
It is connected to by hydrocarbon component conveyance conduit between stripper and pre- chilling tower, the hydro carbons group for being extracted process water extraction tower
Divide and is recycled to pre- chilling tower；
The process steam generator and the process water extraction tower pass through for conveying the hydrocarbon component that extracted
The conveyance conduit of water is connected to, and the process steam generator is used to convert the water for having extracted hydrocarbon component to steam；
The process steam knockout drum is connected to the process steam generator by steam conveying pipe, and the technique is steamed
Vapour knockout drum is used to detach the drop containing salt of entrained in the steam inputted by the steam conveying pipe, to obtain technique steaming
Vapour；Preferably, demister is equipped in the process steam knockout drum；
The process steam input port of the process steam knockout drum and the process water extraction tower is conveyed by process steam
Pipeline is connected to, and at least partly process steam obtained by process steam knockout drum is fed through process water extraction tower.
In some preferred embodiments of the invention, the methanol recovery unit includes that methanol distillation column and methanol distillation column return
Flow tank；
Wherein, the methanol distillation column is connected to the chilling water separation tank by the second chilled water (chw) conveyance conduit, described
Second chilled water (chw) conveyance conduit is used for at least partly described condensed water for having detached heavy hydrocarbon component obtained by chilling water separation tank
It is input to methanol distillation column, the methanol distillation column is used to carry out to inputting the condensed water for having detached heavy hydrocarbon component therein
Rectifying, to obtain process water and the liquid phase component containing methanol and DME；Preferably, the methanol distillation column and the technique are steamed
Vapour generator is connected to by sewage running piping, and the sewage running piping is used to convey the dirt of process steam generator discharge
Water, the methanol distillation column are additionally operable to receive the sewage conveyed by the sewage running piping and carry out rectifying to it, with
Obtain process water and the liquid phase component containing methanol and DME (dimethyl ether)；
The methanol distillation column return tank is connected to the methanol distillation column by liquid phase component conveyance conduit, the methanol
Recovery tower return tank is used to detach to inputting liquid phase component therein, to obtain methanol, DME and light component fixed gas；
Preferably, it is connected with reflux line between the methanol distillation column return tank and the methanol distillation column, described time
Flow tube road is used at least partly methanol and DME that methanol distillation column return tank separation obtains being back to the Methanol Recovery
Tower.
Second aspect of the present invention provide it is a kind of using piece-rate system described above to process for preparing propylene from methanol products therefrom
In the method that is detached of oil-water-gas, the method includes：
The logistics of reaction product containing MTP and dilution steam generation is detached using the hydrocarbon-water separative element, to obtain gas
State hydrocarbon, heavy hydrocarbon component and the condensed water for having detached heavy hydrocarbon component；
Using the oil-gas separative element in the hydrocarbon-water separative element separating obtained gaseous hydrocarbon and heavy hydrocarbon component
The water of entrained with is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；
Utilize the process steam production unit at least partly described separation separating obtained to the hydrocarbon-water separative element
The condensed water of heavy hydrocarbon component is stripped, to isolate wherein remaining hydrocarbon component；And the hydrocarbon component will be extracted
Water handled, isolate the drop containing salt wherein carried secretly, obtain process steam；
It is weighed using the methanol recovery unit at least partly described detached separating obtained to the hydrocarbon-water separative element
The condensed water of the hydrocarbon component is handled, and separation obtains methanol, DME and light component fixed gas.
In the present invention, reaches MTP reaction products in hydrocarbon-water separative element and detached with reaction water and process water.
In some preferred embodiments of the invention, the hydrocarbon-water separative element includes pre- chilling tower, chilling tower and chilled water (chw)
Knockout drum；The pre- chilling tower is equipped with first entrance and second entrance, and the first entrance is located above the second entrance；Institute
It states chilling tower and is equipped with third entrance and the 4th entrance, the third entrance is located at the 4th entrance top, the method includes：
The logistics of reaction product containing MTP and dilution steam generation is fed through pre- chilling tower by the second entrance, by chilled water (chw)
Pre- chilling tower is fed through by the first entrance with lye, the logistics of the reaction product containing MTP and dilution steam generation enters pre- urgency
After cold tower, being contacted with chilled water (chw) and lye from bottom to top is able to cool down and wash, and obtains gaseous stream, heavy hydrocarbon component and condensation
Water；The lye is specifically as follows NaOH solution etc., and the concentration of lye is preferably 15-60wt%.
The gaseous stream that pre- chilling tower obtains is fed through chilling tower via the 4th entrance, by chilled water (chw) and lye by
The third entrance is fed through chilling tower, and the gaseous stream enters after chilling tower from bottom to top abundant with chilled water (chw) and lye
Contact is able to cool down and wash, and is preferably cooled to 35-70 DEG C, more preferable 40-55 DEG C, obtains gaseous hydrocarbon, heavy hydrocarbon component and condensation
Water；
Condensed water obtained by the pre- chilling tower and chilling tower is fed through chilling water separation tank, is isolated residual in condensed water
The heavy hydrocarbon component stayed, and obtain the condensed water for having detached heavy hydrocarbon component；
In some preferred embodiments of the invention, at least partly described of chilling water separation tank acquisition has detached heavy hydrocarbon
The condensed water of component is recycled to the pre- chilling tower and chilling tower as chilled water (chw).In a kind of preferred embodiment,
90-96% (quality) condensed waters for having detached heavy hydrocarbon component that the chilling water separation tank obtains are recycled to as chilled water (chw)
The pre- chilling tower and chilling tower.
Preferably, the logistics of the reaction product containing MTP and dilution steam generation carries out heat before being sent into the pre- chilling tower
Amount recycling, and its temperature is controlled at 170-210 DEG C；
Preferably, the temperature of chilled water (chw) used in the pre- chilling tower and lye is 48-52 DEG C；It is fed through the chilling
The temperature of the gaseous stream from the pre- chilling tower of tower is 50-60 DEG C；Chilled water (chw) and lye used in the chilling tower
Temperature be 38-42 DEG C.
In the present invention, reach the separation of oil and gas that MTP reactions generate, one-step removal of going forward side by side in oil-gas separative element
Wherein remaining water.
In some preferred embodiments of the invention, the oil-gas separative element includes compressor buffer tank, compressor and oil
Gas knockout drum；The method includes：
The separating obtained gaseous hydrocarbon of the chilling tower is fed through compressor buffer tank, isolates and is carried secretly in the gaseous hydrocarbon
Water, obtain liquid material and detached entrainment water gaseous hydrocarbon；Preferably, the liquid material is fed through in chilling tower；
The gaseous hydrocarbon of the water for having detached entrainment obtained by the compressor buffer tank is fed through compressor, it is compressed
After machine compresses and cools down, gas mixture is obtained.The control of preferred compressed machine outlet pressure is 2.0-2.5MPa, the preferably described cooling
To cool the temperature to 35-50 DEG C.
The gas mixture and pre- chilling tower that the compressor obtains, chilling tower and chilling water separation tank are detached
To heavy hydrocarbon component be fed through catch pot, isolate the water wherein carried secretly, obtain gaseous component, hydrocarbon lime set and remaining
Water；
Preferably, the remaining water is fed through compressor buffer tank.Preferably, hydrocarbon lime set is sent into next separative element
To isolate C4, C5-6 component therein, the gaseous component is sent into next stage compression unit.
In the present invention, in process steam production unit production technology steam, the remaining hydrocarbon component of one-step removal of going forward side by side and
Isolate the drop containing salt (such as drop containing sodium salt) that may be carried secretly.The process steam of production may return to MTP reactors.
In some preferred embodiments of the invention, the process steam production unit includes process water extraction tower, technique steaming
Vapour generator and process steam knockout drum；The method includes：
At least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is fed through described
Process water extraction tower inputs process steam into process water extraction tower, and the process steam pair is utilized in process water extraction tower
The condensed water for having detached heavy hydrocarbon component is stripped, to isolate wherein remaining hydrocarbon component, obtain hydrocarbon component and
The water of hydrocarbon component is extracted；Preferably, the separating obtained hydrocarbon component of the process water extraction tower is recycled to pre- chilling tower；
Preferably, at least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is entering the technique
It before water extraction tower, is pressurizeed using chilling water pump and (is preferably forced into 0.4~1.2MPa), and filtered to detach therein
Grain object.In some preferred embodiments, by 4-10% (quality) described separation of chilling water separation tank acquisition
The condensed water of heavy hydrocarbon component is fed through the process water extraction tower.
The water for having extracted hydrocarbon component obtained by process water extraction tower is fed through process steam generator, is steamed
Vapour；Preferably, the water for having extracted hydrocarbon component is pressurizeed and is preheated before being sent into the process steam generator,
It is preferred that being preheated to 180-250 DEG C；Wherein, the pressurization can be pressurizeed using water pump (such as technique water pump),
It is preferred that being forced into 1.0~2.6MPa.
The steam that the process steam generator generates is fed through process steam knockout drum, isolates and is carried secretly in steam
Drop containing salt (such as drop containing sodium salt) obtains process steam；In specific implementation mode, it can pacify in process steam generator
Demister is filled to effectively remove the drop containing salt that may be carried secretly in steam.
At least partly process steam that the process steam generator obtains is input to process water extraction tower.It is specifically logical
The process steam entrance for crossing process water extraction tower enters wherein, is not necessarily to additional supply process steam.Preferably it is being embodied
In mode, after also some processes steam is mixed and heated to 430 DEG C as dilution steam generation and recycle hydrocarbons and DME, it is anti-to be fed through MTP
Answer device.In the present invention, the unreacted methanol in methanol recovery unit, recovery process water, and isolate light component fixed gas.
In some preferred embodiments of the invention, the methanol recovery unit includes that methanol distillation column and methanol distillation column return
Flow tank；The method includes：
At least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is fed through methanol
Recovery tower detaches through rectifying and obtains process water and the liquid phase component containing methanol and DME；Preferably, also by the process steam
The sewage (process steam generator meeting discharge part sewage while generating steam) of generator discharge is fed through the methanol
Recovery tower carries out rectifying, to obtain process water and the liquid phase containing methanol and DME；In a kind of preferred embodiment,
The sewage of process steam generator discharge is mutually exchanged with the condensed water for having detached heavy hydrocarbon component from chilling water separation tank
The methanol distillation column is mixed into after heat；In preferred embodiment, by the work of methanol distillation column rectifying separation acquisition
Skill water send after cooling to oxide extraction unit and uses.
The liquid phase component obtained by methanol distillation column is fed through methanol distillation column return tank, separation obtains methanol, DME
With light component fixed gas；Separating obtained at least partly methanol and DME are back to the methanol distillation column.Preferred specific
In embodiment, the methanol and DME that are also partially separated gained are back to DME reactors, separating obtained light component fixed gas
It is recycled back to MTP reactors.
In some preferred embodiments, both pre- chilling tower and chilling tower structure used in piece-rate system of the invention
The tower structure disclosed in patent CN202860169U may be used；Process steam point used in the piece-rate system of the present invention
The steam tower structure disclosed in patent CN204328982U or CN202191808U may be used from tank.
Technical solution provided by the invention has the advantages that：
The piece-rate system of the present invention, passes through hydrocarbon-water separative element, oil-gas separative element, process steam production unit and first
The ingenious combination of the multi-stage separation unit of alcohol recovery unit is addressed in conventional art that there are gas, oil and water separating effects not
Good problem.By the present invention piece-rate system can effectively by methanol to propylene reaction product (MTP reaction products) with react
Water, process water are kept completely separate, and MTP reactor outlet logistics is separated into oil, water and gas, it is more thorough to reach oil-water-gas
The separation at bottom to ensure that subsequent gases compressibility is run, and avoids the drying of follow-up hydrocarbon product there are larger difficulty, together
When also ensured the long period even running of MTP process units, avoid causing to jump vehicle accident.
In the preferred embodiment of the present invention, detached with process steam using process steam generator in process steam production unit
The mode that tank is combined, further remove steam in small droplet, ensured salt drop especially sodium contained in steam from
Son is effectively removed.
The advantages such as the separation method of the present invention has simple and reliable process, and stability is good.
Description of the drawings
Fig. 1 is the showing in one embodiment of oil-water-gas separating system for process for preparing propylene from methanol of the present invention
It is intended to.
Specific implementation mode
For a better understanding of the technical solution of the present invention, with reference to the embodiment content that the present invention is further explained,
But present disclosure is not limited only to following embodiment.
As shown in Figure 1, a kind of oil-water-gas separating system for process for preparing propylene from methanol, including hydrocarbon-water separative element
100, oil-gas separative element 200, process steam production unit 300 and methanol recovery unit 400.
Wherein, hydrocarbon-water separative element 100 is for detaching the logistics of reaction product containing MTP and dilution steam generation, the object
The input of material conveying pipe 1 is flowed through, gaseous hydrocarbon, heavy hydrocarbon component are obtained through hydrocarbon-separation of water separative element 100 and has detached heavy hydrocarbon group
The condensed water divided.
In some preferred embodiments, hydrocarbon-water separative element 100 is mainly by pre- chilling tower 101, chilling tower 102 and urgency
Cold water knockout drum 103 forms.
Wherein, pre- chilling tower 101 is equipped with first entrance for inputting chilled water (chw) and lye, and the first of pre- chilling tower 101
Entrance is connected to lye conveyance conduit 11, can be directly connection or indirect communication, lye is inputted it through lye conveyance conduit 11
In；The first entrance of pre- chilling tower 101 is also connected to chilled water (chw) conveyance conduit 2, inputs chilled water (chw) through chilled water (chw) conveyance conduit 2
Wherein.In a specific embodiment, lye conveyance conduit 11 and chilled water (chw) conveyance conduit 2 communicate, and lye and chilled water (chw) converge
Enter pre- chilling tower 101 through first entrance after entering to same pipeline.Pre- chilling tower 101 is additionally provided with for inputting containing MTP reaction productions
The second entrance of the logistics of object and dilution steam generation, the second entrance are connected to material conveying pipe 1, and the first of pre- chilling tower 101
Entrance is located above second entrance." first entrance " and " second entrance " described herein is merely for convenience of distinguishing and describe not
With feed inlet of the material in pre- chilling tower 101, not entrance is ranked up, also not the quantity of its entrance is limited
It is fixed.The logistics of containing MTP reaction product and dilution steam generation of the pre- chilling tower 101 for that will be inputted by second entrance with by first entrance
The chilled water (chw) and lye of input come into full contact with, and the logistics of reaction product containing MTP and dilution steam generation is cooled down and be washed, obtain
Obtain gaseous stream, heavy hydrocarbon component and condensed water.Wherein, lye used can be specifically that the NaOH of concentration 15-60wt% is molten
Liquid.The gaseous stream obtained is mainly made of C1-C5 hydrocarbon mixtures, also contains a small amount of CO, C5+ hydrocarbon etc..Due to first entrance position
Enter pre- chilling tower above second entrance, thus by the reaction product containing MTP of second entrance input and the logistics 1 of dilution steam generation
After 101, with the chilled water (chw) and lye that are inputted by first entrance coming into full contact with from bottom to top.
Chilling tower 102 is equipped with the third entrance for inputting chilled water (chw) and lye, is additionally provided with and comes from pre- chilling for inputting
4th entrance of the gaseous stream of tower 101, third entrance are located at the 4th entrance top." third entrance " described herein and "
Four entrances " are merely for convenience of distinguishing and describing feed inlet of the different material in chilling tower 102, not arrange entrance
Sequence is also not defined the quantity of entrance.In a kind of specific implementation mode, the third entrance and lye of chilling tower 102 are defeated
Pipeline 12 is sent to be connected to, " connection " can be directly or indirectly connection, input lye wherein through lye conveyance conduit 12；Chilling
The third entrance of tower 102 is also connected to chilled water (chw) conveyance conduit 4, inputs chilled water (chw) wherein through chilled water (chw) conveyance conduit 4.One
In kind specific implementation mode, lye conveyance conduit 12 and chilled water (chw) conveyance conduit 4 communicate, and lye and chilled water (chw) are imported to same pipe
Enter chilling tower 102 through third entrance behind road.4th entrance of chilling tower 102 and the gaseous stream outlet of pre- chilling tower 101 are logical
It crosses gaseous stream conveyance conduit 3 to be connected, chilling tower 102 is for entering the gaseous stream from pre- chilling tower 101 with by third
Mouth enters to chilled water (chw) and lye contact in chilling tower 102, to be cooled down to gaseous stream and be washed, acquisition gaseous hydrocarbon,
Heavy hydrocarbon component and condensed water.Since third entrance is located at the 4th entrance top, thus by the gaseous stream of the 4th entrance input into
After entering chilling tower 102, with the chilled water (chw) 4 and lye 12 that are inputted by third entrance coming into full contact with from bottom to top.
Chilling water separation tank 103 is connected by condensed water conveyance conduit 6,7 respectively with pre- chilling tower 101, chilling tower 102
It is logical, it is carried out for receiving the condensed water from pre- chilling tower 101 and chilling tower 102, and to remaining heavy hydrocarbon component in condensed water
Separation, with the condensed water for obtaining heavy hydrocarbon component He having detached heavy hydrocarbon component, the condensed water of separation heavy hydrocarbon component can conduct
Chilled water (chw), thus also the condensed water can be known as chilled water (chw).
In some preferred embodiments, chilling water separation tank 103 respectively with the first entrance of pre- chilling tower 101,
It is connected to by chilling water circulating pipe 10 between the third entrance of chilling tower 102.In a specific embodiment, the chilled water (chw)
Circulating line 10 is connected with chilled water (chw) conveyance conduit 2,4 respectively, and then the separation of chilling water separation tank 103 obtains at least partly
The condensed water for having detached heavy hydrocarbon component is recycled to pre- chilling tower 101 and chilling tower 102 as chilled water (chw) respectively.It is specific real at some
It applies in mode, the condensed water that the major part (such as 90-96%) that the separation of chilling water separation tank 103 obtains has detached heavy hydrocarbon component is made
For in chilled water (chw) circulation-supplied to pre- chilling tower 101 and chilling tower 102.
MTP reaction products are detached with reaction water and process water by hydrocarbon-water separative element 100.
Oil-gas separative element 200 in piece-rate system be used for hydrocarbon-separating obtained gaseous hydrocarbon of water separative element 100 and
The water of entrained with is detached in heavy hydrocarbon component, to obtain gaseous component, hydrocarbon lime set and remaining water.Wherein, gaseous hydrocarbon is main
It is made of C1-C5 hydrocarbon mixtures.Heavy hydrocarbon component is mainly made of C5-C11 hydrocarbon mixtures.Gaseous component is mainly by C1-C4 hydrocarbon mixture groups
At.
In some preferred embodiments, oil-gas separative element 200 is mainly by compressor buffer tank 201, compressor 203
It is formed with catch pot 202.Wherein, compressor buffer tank 201 is used for the water to being carried secretly in the gaseous hydrocarbon from chilling tower 102
It is detached, to obtain liquid material and detach the gaseous hydrocarbon for the water carried secretly.As a preferred embodiment, compressor
It is connected to by gaseous hydrocarbon conveyance conduit 5 between surge tank 201 and chilling tower 102, through gaseous hydrocarbon conveyance conduit 5 by chilling tower 102
The gaseous hydrocarbon of acquisition is input to compressor buffer tank 201.In a specific embodiment, compressor buffer tank 201 and chilling
Liquid material conveyance conduit 9 is also associated between tower 102, to which the liquid material for obtaining the separation of compressor buffer tank 201 follows
Ring is further detached to chilling tower 102.
Gaseous hydrocarbon of the compressor 203 for the water of the separation separating obtained to compressor buffer tank 201 entrainment is pressed
Contracting and cooling, are specifically such as cooled to 35~60 DEG C, to obtain gas mixture 33.In a kind of specific embodiment, compressor
It is connected to by pipeline 31 between 203 and compressor buffer tank 201, the separating obtained separation of compressor buffer tank 201 is pressed from both sides
The gaseous hydrocarbon of the water of band is fed through compressor 203.
It is connected to by gas mixture conveyance conduit 33 between catch pot 202 and compressor 203.Catch pot
202 also pass through heavy hydrocarbon component conveyance conduit 17,16,8 respectively with pre- chilling tower 101, chilling tower 102 and chilling water separation tank 103
Connection.In a specific embodiment, heavy hydrocarbon component conveyance conduit 17,16,8 can be imported to same pipeline, will come from three
Heavy hydrocarbon component converge feeding catch pot.Catch pot 202 be used for from compressor 203 gas mixture and point
The minor amount of water that may be carried secretly in heavy hydrocarbon component not from pre- chilling tower 101, chilling tower 102 and chilling water separation tank 103 carries out
Separation, and obtain gaseous component, hydrocarbon lime set and remaining water.
In a specific embodiment, to be connected with residual water between catch pot 202 and compressor buffer tank 201 defeated
Pipeline 28 is sent, is further divided for remaining water isolated in catch pot 202 to be fed through compressor buffer tank 201
From.It can further include next oxide extraction unit (not shown), the separating obtained hydrocarbon of catch pot 202
Lime set is fed through the oxide extraction unit by hydrocarbon lime set conveyance conduit 29, which is used for will be in hydrocarbon lime set
C4, C5-6 the oxygen-bearing organic matter component contained is stripped separation.It is existing that this field may be used in the oxide extraction unit
Extracting separative element isolates C4, C5-6 methanol/dimethyl ether component from hydrocarbon lime set, is repeated no more to this.Under can also including
Level-one separative element (not shown) is conveyed between catch pot 202 and the next stage separative element by gaseous component
Pipeline 30 is connected to；The next stage separative element makes it further for receiving the separating obtained gaseous component of catch pot 202
Separation obtains C2 and C3 components.
Mainly reach the separation of oil and gas that MTP reactions generate by oil-gas separative element 200, and further takes off
Except wherein remaining water, the progress of the processes such as drying, compression to be conducive to follow-up the hydrocarbon component.
Process steam production unit 300 be used for by hydrocarbon-water separative element 100 it is separating obtained be at least partially separate heavy hydrocarbon
The remaining hydrocarbon component of institute is stripped in the condensed water of component, to the water for obtaining hydrocarbon component He having extracted hydrocarbon component；
It is additionally operable to handle in the water for having extracted hydrocarbon component to isolate the drop containing salt wherein carried secretly, to obtain separation
The process steam of the drop containing salt.
In a specific embodiment, process steam production unit 300 is mainly steamed by process water extraction tower 301, technique
Vapour generator 302 and process steam knockout drum 303 form.
Wherein, connected by the first chilled water (chw) conveyance conduit 14 between process water extraction tower 301 and chilling water separation tank 103
It is logical, through the first chilled water (chw) conveyance conduit 14 by the condensation for being at least partially separate heavy hydrocarbon component of 103 gained of chilling water separation tank
Water is input to process water extraction tower 301.Process water extraction tower 301 is additionally provided with process steam input port, for being extracted to process water
Process steam is inputted in tower 301.Process water extraction tower 301 is used at least partly divide chilling water separation tank 103 is separating obtained
Condensed water from heavy hydrocarbon component is contacted with process steam, and to extract wherein remaining hydrocarbon component, acquisition has extracted hydrocarbon
The water and hydrocarbon component of class component.In a kind of preferred embodiment, process water extraction tower 301 and pre- chilling tower 101
Between be connected with hydrocarbon component conveyance conduit 15, further divide for the hydrocarbon component isolated to be recycled to pre- chilling tower 101
From processing.In a specific embodiment, it is additionally provided with chilled water (chw) between chilling water separation tank 103 and process water extraction tower 301
Pump and filter plant (not shown) are respectively used to the heavy hydrocarbon component that detached to that will input process water extraction tower 301
Condensed water is pressurizeed and is filtered, and particulate matter therein is detached.
Process steam generator 302 is used for having extracted at the water of hydrocarbon component from process water extraction tower 301
Reason, to generate steam.Specifically, process steam generator 302 is connected to process water extraction tower 301 by conveyance conduit 27,
The water for having extracted hydrocarbon component is fed through process steam generator 302 through the conveyance conduit 27.In process steam generator 302
Occur to will produce part of contaminated water during steam.The sewage is discharged through sewage running piping 19, is sent into subsequent Methanol Recovery
It is further processed in unit 400.In a kind of preferred embodiment, in process steam generator and process water extraction tower
Between be additionally provided with water pump (specific as technique water pump) and pre-heating device (not shown), be respectively used to technique will be input to
The water for having extracted hydrocarbon component of steam generator 302 is pressurizeed and is preheated, such as is preheated to 170-250 DEG C.
Process steam knockout drum 303 is isolated for handling the steam from process steam generator 302 from the steam
The drop containing salt (such as drop containing sodium salt) that may wherein carry secretly, to obtain process steam.Specifically, process steam detaches
It is connected to by steam conveying pipe 18 between tank 303 and process steam generator 302, is sent into steam by steam conveying pipe 18
To process steam knockout drum 303.In a kind of preferred embodiment, foam removal is installed in process steam knockout drum 303
Device efficiently separates drop containing salt, and this field, which may be used, arbitrarily in demister has the device of the separation effect of drop containing salt.
In a kind of specific implementation mode, process steam is equipped between process steam knockout drum 303 and process water extraction tower 301
Conveyance conduit 20 should for at least partly process steam obtained by process steam knockout drum to be fed through process water extraction tower 301
Some processes steam 20 is specifically entered by the process steam entrance of process water extraction tower 301 wherein, because without additionally to technique
Process steam is supplied in water extraction tower 301.In a preferred embodiment, also some processes steam passes through process steam
Conveyance conduit 21 exports and is recycled to MTP reactors, is specifically such as mixed and heated to some processes steam and recycle hydrocarbons and DME
After 430 DEG C, it is fed through MTP reactors.
Process water extraction tower 301 and MTP reactors can be supplied by obtaining process steam through process steam production unit 300,
And further it is stripped of remaining hydrocarbon component and the drop containing salt that may be carried secretly (such as liquid containing sodium salt in the unit
Drop).
Methanol recovery unit 400 has been at least partially separate heavy hydrocarbon component for separating obtained to hydrocarbon-water separative element 100
Condensed water handled, to isolate methanol contained therein, DME and light component fixed gas.
In some embodiments, methanol recovery unit 400 is mainly returned by methanol distillation column 401 and methanol distillation column
Tank 402 is flowed to form.
Wherein, it is connected to by the second chilled water (chw) conveyance conduit 13 between methanol distillation column 401 and chilling water separation tank 103,
To which the condensed water for being at least partially separate heavy hydrocarbon component for obtaining the separation of chilling water separation tank 103 inputs methanol distillation column
401, carry out rectifying in methanol distillation column 401, obtain the liquid phase component (or referred to as " liquid phase ") containing methanol and DME and
Process water.In a preferred embodiment, methanol distillation column 401 also passes through sewage running piping with process steam generator
19 connections can be that directly connection or indirect communication, the sewage for receiving the discharge of process steam generator 302 carry out essence to it
It evaporates, isolates the liquid phase component containing methanol and DME, and obtain process water.In a kind of preferred embodiment, sewage
Conveyance conduit 19 is connected to the second chilled water (chw) conveyance conduit 13, the sewage and come from chilled water (chw) that process steam generator 302 is discharged
The condensed water for having detached heavy hydrocarbon component of knockout drum 103 is imported to same conveyance conduit, and the two mutually exchanges heat, and is mixed into methanol
Recovery tower 401.The process water obtained by 401 rectifying of methanol distillation column separation, which can be also sent after cooling to subsequent oxide, to be extracted
Unit uses.
It is connected to, is used for by liquid phase component conveyance conduit 22 between methanol distillation column return tank 402 and methanol distillation column 401
The liquid phase component of 401 gained of methanol distillation column is received, and it is detached, isolates methanol and DME therein and light group
Divide fixed gas.In a kind of preferred embodiment, it is also associated with back between methanol distillation column return tank 402 and methanol distillation column 401
Flow tube road 25, in a kind of specific embodiment, reflux line is connected (not shown) with reflux pump, passes through reflux line 25
At least partly methanol and DME that the separation of methanol distillation column return tank 402 obtains are back to methanol distillation column 401.Preferred
In specific implementation mode, also it is partially separated the methanol of gained and DME can be used as raw material and be back to DME reactions through conveyance conduit 26
Device (not shown), and separating obtained light component fixed gas can also export and recycle through light component fixed gas conveyance conduit 23
Return MTP reactor (not shown)s.
It through methanol recovery unit 400, is able to separate and recover unreacted methanol in process water, while also separation obtains
Obtain light component fixed gas.
In piece-rate system provided by the present invention, specific equipment or element used in each separative element can be adopted specifically
With the existing relevant device in this field or element, this is not repeated one by one.And in some preferred embodiments, piece-rate system
Used in both pre- chilling tower 101 and chilling tower 102 structure the tower disclosed in patent CN202860169U may be used
Structure；Process steam knockout drum 303 used may be used disclosed in patent CN204328982U or CN202191808U
Steam tower structure.
The present invention also provides carried out to oil-water in process for preparing propylene from methanol products therefrom-gas using above-mentioned piece-rate system
The method of separation.This method includes：
The logistics of reaction product containing MTP and dilution steam generation is detached using hydrocarbon-water separative element 100, obtains gaseous state
Hydrocarbon, heavy hydrocarbon component, and detached the condensed water of heavy hydrocarbon component；
Using oil-gas separative element 200 to hydrocarbon-water separative element 100 to folded in the gaseous hydrocarbon and heavy hydrocarbon component of gained
The water of band is detached, and gaseous component, hydrocarbon lime set and remaining water are obtained；
Utilize at least partly described separation separating obtained to hydrocarbon-water separative element 100 of process steam production unit 300
The condensed water of heavy hydrocarbon component is stripped, and wherein remaining hydrocarbon component is isolated through extracting；And hydrocarbon component will be extracted
Water is handled, and isolates the drop containing salt that may wherein carry secretly, and obtain process steam；
Utilize the separation of at least partly front gained separating obtained to hydrocarbon-water separative element 100 of methanol recovery unit 400
The condensed water of heavy hydrocarbon component is handled, to isolating methanol contained therein and DME and light component fixed gas, and
Obtain process water.
In some preferred embodiments, hydrocarbon-water separative element 100 includes mainly pre- chilling tower 101,102 and of chilling tower
Chilling water separation tank 103.
Wherein pre- chilling tower 101 is equipped with first entrance and second entrance, and first entrance is located above second entrance；Chilling tower
102 are equipped with third entrance and the 4th entrance, and third entrance is located at the 4th entrance top.
The separation method of the present invention is in hydrocarbon-water separative element 100, by the logistics of reaction product containing MTP and dilution steam generation
It is sent into wherein, by chilled water (chw) and lye by pre- chilling tower 101 by second entrance of the material conveying pipe 1 through pre- chilling tower 101
First entrance is sent into wherein；The logistics of reaction product containing MTP and dilution steam generation enter pre- chilling tower 101 after from bottom to top with urgency
Cold water and lye contact obtain gaseous stream, heavy hydrocarbon component and condensed water to be cooled down and be washed.It is preferably specific at some
In embodiment, MTP reaction products specifically come from MTP reactors, and the logistics of reaction product containing MTP and dilution steam generation is being sent into advance
Before chilling tower 101, heat recovery is first carried out, and is about 170~210 DEG C by the control of its temperature, is re-fed into pre- chilling tower later
In 101.Preferably, the temperature of chilled water (chw) used in pre- chilling tower 101 and lye is 48-52 DEG C.
The gaseous stream that pre- chilling tower 101 obtains is sent through gaseous stream conveyance conduit 3 by the 4th entrance of chilling tower 102
Enter wherein, chilled water (chw) and lye are sent into wherein by the third entrance of chilling tower 102；Gaseous stream enters after chilling tower 102 certainly
Being contacted with chilled water (chw) and lye on down obtains gaseous hydrocarbon, heavy hydrocarbon component and condensation to further be cooled down and be washed
Water.Preferably, the temperature for being fed through the gaseous stream from the pre- chilling tower of chilling tower 102 is 50-60 DEG C；Chilling tower
The temperature of chilled water (chw) used in 102 and lye is 38-42 DEG C.
By the condensed water of 102 gained of pre- chilling tower 101 and chilling tower, condensed water conveyance conduit 6,7 is fed through chilling respectively
Water separation tank 103 isolates remaining heavy hydrocarbon component in condensed water, and obtains the condensed water for having detached heavy hydrocarbon component.Chilled water (chw)
The condensed water for being at least partially separate heavy hydrocarbon component of the acquisition of knockout drum 103 is recycled as chilled water (chw) through chilling water circulating pipe 10
To pre- chilling tower 101 and chilling tower 102, specifically, having respectively entered chilled water (chw) conveying after being exported by chilling water circulating pipe 10
Pipeline 2,4 is fed through pre- chilling tower and chilling tower.In some preferred embodiments, chilling water separation tank 103 obtains extremely
The condensed water that small part has detached heavy hydrocarbon component is divided into three strands, and wherein one is recycled to pre- 101 He of chilling tower as chilled water (chw)
Chilling tower 102, wherein one be fed through subsequent process water production unit 300, another stock is fed through subsequent Methanol Recovery list
Member 400.In a kind of preferred embodiment, the 90-96% that chilling water separation tank 103 obtains has detached heavy hydrocarbon component
Condensed water is recycled to the pre- chilling tower 101 and chilling tower 102 as chilled water (chw).
In some preferred embodiments, oil-gas separative element 200 includes mainly compressor buffer tank 201, compressor
203 and catch pot 202；The present invention separation method include：
The separating obtained gaseous hydrocarbon of chilling tower 102 is fed through compressor buffer tank 201 through gaseous hydrocarbon conveyance conduit 5, point
The water carried secretly in gaseous hydrocarbon is separated out, liquid material is obtained and has detached the gaseous hydrocarbon of the water of entrainment.In a kind of preferred specific implementation
In mode, liquid material is recycled in chilling tower 102 through liquid material conveyance conduit 9 and further detaches.
The gaseous hydrocarbon of the water of the separation of 201 gained of compressor buffer tank entrainment is fed through compressor through conveyance conduit 31
203, it compresses and cools down through compressor 203, after being specifically such as cooled to 35~60 DEG C, obtain gas mixture.
The gas mixture that compressor 203 is obtained is sent into catch pot 202 through gas mixture conveyance conduit 33, will
Pre- chilling tower 101, chilling tower 102 and the isolated heavy hydrocarbon component of chilling water separation tank 103 are respectively through heavy hydrocarbon component delivery pipe
Road 17,16,8 exports and is fed through catch pot 202, isolates the water that may wherein carry secretly, obtains gaseous component, hydrocarbon lime set
With remaining water.In some preferred specific implementation modes, remaining water is further fed through pressure through residual water conveyance conduit 28
Contracting machine surge tank 201 is detached.In some preferred specific implementation modes, hydrocarbon lime set can also continue to be sent into next separation list
First (not shown), to isolate C4, C5-6 component therein；Gaseous component 30 can also be sent into next stage separative element
(not shown) makes it further detach and obtains C2 and C3 components.
In some preferred embodiments, process water production unit 300 includes mainly process water extraction tower 301, technique steaming
Vapour generator 302 and process steam knockout drum 303.The present invention separation method include：
The condensed water for being at least partially separate heavy hydrocarbon component that chilling water separation tank 103 obtains is conveyed through the first chilled water (chw)
Pipeline 14 is fed through process water extraction tower 301, and the chilling water input through process water extraction tower 301 is sent into wherein, and technique is steamed
Process steam input port input of the vapour through process water extraction tower 301 is wherein.In a kind of preferred embodiment, by chilling
The condensed water that 28~42wt% that water separation tank 103 obtains has detached heavy hydrocarbon component is fed through through the first chilled water (chw) conveyance conduit 14
Process water extraction tower 301.The condensed water for having detached heavy hydrocarbon component is taken out using process steam in process water extraction tower 301
It carries, to isolate wherein remaining hydrocarbon component, obtains hydrocarbon component and extracted the water of hydrocarbon component.It is preferred at some
In specific implementation mode, the separating obtained hydrocarbon component of process water extraction tower 301 is recycled to through hydrocarbon component conveyance conduit 15
Pre- chilling tower 101 further detaches.In some preferred embodiments, at least portion of the acquisition of chilling water separation tank 103
The condensed water of heavy hydrocarbon component has been detached before entering process water extraction tower 301, has been pressurizeed in advance using chilling water pump, and
It is filtered to detach the particulate matter that may wherein contain.
By the water for having extracted hydrocarbon component of 301 gained of process water extraction tower, process steam is fed through through conveyance conduit 27
Generator 302 obtains steam in process steam generator 302.In a preferred embodiment, hydrocarbon component has been extracted
Water before being sent into process steam generator 302, pressurizeed and preheated using water pump (such as technique water pump), preferably
It is preheated to 140-150 DEG C.
The steam that process steam generator 302 generates is fed through process steam knockout drum 303 through steam conveying pipe 18,
The drop containing salt (such as drop containing sodium salt) that may be carried secretly in steam is isolated, process steam is obtained.
At least partly process steam that process steam knockout drum 303 obtains is fed through work through process steam conveyance conduit 20
Skill water extraction tower 301 enters wherein particular by the process steam entrance of process water extraction tower 301, without being taken out to process water
Extra Supply process steam in stripper 301.In a preferred embodiment, also some processes steam is defeated through process steam
After sending pipeline 21 to be mixed and heated to 430 DEG C with recycle hydrocarbons and DME as dilution steam generation, it is fed through the use of MTP reactors.
In some preferred embodiments, methanol recovery unit 400 includes mainly methanol distillation column 401 and methanol distillation column
Return tank 402.The present invention separation method include：
The condensed water for being at least partially separate heavy hydrocarbon component that chilling water separation tank 103 obtains is conveyed through the second chilled water (chw)
Pipeline 13 is fed through methanol distillation column 401, and rectifying separation is carried out in methanol distillation column 401, isolates containing methanol and DME
Liquid phase component, and obtain process water.In a kind of preferred embodiment, also process steam generator 302 is discharged
Sewage, which exports through sewage running piping 19 and is fed through methanol distillation column 401, carries out rectifying, isolates and wherein contains methanol and DME
Liquid phase component, and obtain process water.In a kind of preferred embodiment, the dirt of the discharge of process steam generator 302
Water is mixed into methanol distillation column after mutually exchanging heat with the condensed water for having detached heavy hydrocarbon component from chilling water separation tank 103
401.In preferred embodiment, the process water obtained by 401 rectifying of methanol distillation column separation after cooling can be by technique
Water conveyance conduit 24 send into subsequent oxide extraction unit and uses.
The liquid phase component containing methanol and DME of 401 gained of methanol distillation column is sent into through liquid phase component conveyance conduit 22
To methanol distillation column return tank 402, methanol and DME and light component fixed gas therein are isolated.By it is separating obtained at least
Part methanol and DME are back to methanol distillation column through reflux line 25.In a preferred embodiment, it is also partially separated
The methanol and DME of gained are back to DME reactors as reaction raw materials through conveyance conduit 26 and use, and separating obtained light component is not
Solidifying gas can be recycled back to MTP reactors through light component fixed gas conveyance conduit 23.
1 pair of piece-rate system using the present invention is to the oil-in the reaction product of process for preparing propylene from methanol below in conjunction with the accompanying drawings
The technical process that water-gas is detached carries out citing detailed description：
The logistics of the reaction product and dilution steam generation that are come out from the MTP reactors of upstream recycles heat through heat recovery system
Afterwards, temperature drops to about 190 DEG C, enters pre- chilling tower 101 through material conveying pipe 1, with 48~52 DEG C of chilled water (chw)s and lye pre-
It comes into full contact with, cool down, wash in chilling tower 101, acquisition is cooled to 50-60 DEG C of gaseous stream and condensed water；Gaseous stream passes through
Gaseous stream conveyance conduit 3 enters chilling tower 102, further comes into full contact with, cools down, washes with 38~42 DEG C of chilled water (chw)s and lye
It washs.Most of heavy hydrocarbon component is condensed out in pre- chilling tower 101 and chilling tower 102, respectively obtains heavy hydrocarbon component, and respectively by weight
The hydrocarbon component conveyance conduit 17,16 exports.
From 102 top of chilling tower, gaseous hydrocarbon out enters compressor buffer tank 201 through gaseous hydrocarbon conveyance conduit 5, into one
The drop (water) that step removing may wherein carry secretly.
The condensed water that the condensed water come out from pre- 101 bottom of chilling tower and 102 bottom of chilling tower come out is respectively by condensed water
Conveyance conduit 6,7 exports and fully enters chilling water separation tank 103, and oily (hydrocarbon) water separation is carried out by gravity.It isolates
Remaining heavy hydrocarbon component therein, and the condensed water for having detached heavy hydrocarbon component is obtained, which is allocated as three strands, wherein most
It is recycled in system as chilled water (chw), is recycled to pre- chilling tower and chilling tower；Specifically, chilled water (chw) warp of this part for cycle
Heat recovery and air-cooled postcooling are crossed to after 50 DEG C, is exported through chilling water circulating pipe 10, and continue to be allocated as two strands, wherein big portion
It is allocated as entering chilled water (chw) conveyance conduit 2 for chilled water (chw) and input in pre- chilling tower 101, fraction chilled water (chw) is further cooled to 38 DEG C
Enter chilling tower 102 through chilled water (chw) conveyance conduit 4, further cooling MTP reaction products, to which 102 tower top of chilling tower will be left
Gaseous hydrocarbon in water content minimize.
The condensed water that heavy hydrocarbon component has been detached described in the fraction isolated from chilling water separation tank 103 is passed through as chilled water (chw)
After chilling water pump pressurizes and filters, the particulate matter gathered in chilled water (chw) is removed, is delivered to through the first chilled water (chw) conveyance conduit 14
Process water extraction tower 301, the condensed water that has detached heavy hydrocarbon component of the remainder from chilling water separation tank 103 is through the second chilling
Water conveyance conduit 13 is sent into methanol distillation column 401.
The liquid stream isolated from 201 bottom of compressor buffer tank is back to chilling tower through liquid stream conveyance conduit 9
102.The gaseous hydrocarbon of separation from the top of compressor buffer tank 201 water of entrainment enters compressor 203 through conveyance conduit 31
After being compressed and being cooled to 50 DEG C, gas mixture is obtained, gas mixture is sent into oil through gas mixture conveyance conduit 33
Gas knockout drum 202.
Heavy hydrocarbon component that pre- chilling tower 101 is isolated, chilling tower 102 condensation and separation of heavy hydrocarbon component, chilled water (chw) detaches
The heavy hydrocarbon component that tank 103 is isolated is exported through heavy hydrocarbon component conveyance conduit 17,16,8 and is sent to catch pot 202 respectively, into
One step isolates the water that may be carried secretly.
Hydrocarbon lime set and remaining water detach in catch pot 202 with gaseous component.Gaseous component is defeated through gaseous component
It send pipeline 30 to export, next stage separative element (not shown) can be continued to be fed into；Hydrocarbon lime set is defeated through hydrocarbon lime set conveyance conduit 29
Go out, next separative element (such as oxide extraction unit) can be sent into isolate C4, C5-6 oxygen-bearing organic matter component and (not show in figure
Go out), these component Parts or all return MTP reactors；Remaining water is sent into compressor through residual water conveyance conduit 28 and is delayed
Rush tank 201.
In process water extraction tower 301, using the process steam from process steam knockout drum 303 to having detached heavy hydrocarbon group
The condensed water divided (alternatively referred to as " chilled water (chw) ") is stripped.The hydrocarbon component extracted is returned through hydrocarbon component conveyance conduit 15
To pre- chilling tower 101.Chilled water (chw) (water for having extracted hydrocarbon component) after extracting is preheated to 140 after being pressurizeed by technique water pump
It~150 DEG C, is sent into process steam generator 302 through conveyance conduit 27 and steam occurs, the steam of production is through steam conveying pipe
18 enter process steam knockout drum 303.In the process steam knockout drum 303 for installing demister additional, what may be carried secretly in steam contains
Salt drop is separated.
The sewage that process steam generator 302 is discharged is through sewage running piping 19 and remaining from chilling water separation tank 103
The remaining condensed water for being partially separated heavy hydrocarbon component is mixed into methanol distillation column 401 after mutually exchanging heat, and carries out rectifying wherein.
The process steam part that 303 top of process steam knockout drum is flowed out is sent into process water extraction tower through process steam conveyance conduit 20
301, another part process steam mixes addition with recycle hydrocarbons and DME extremely through process steam conveyance conduit 21 as dilution steam generation
After 430 DEG C, it is sent into MTP reactors.
The condensed water that has detached heavy hydrocarbon component of the part from chilling water separation tank 103 is through the second chilled water (chw) conveyance conduit 13
It is sent into methanol distillation column 401 and isolates methanol and DME contained therein, and in tower top through rectifying in methanol distillation column 401
Condensation obtains the liquid phase component 22 containing methanol and DME.The liquid phase component of overhead condensation enters first through liquid phase component conveyance conduit 22
Alcohol recovery tower return tank 402.The methanol and DME isolated from methanol distillation column return tank 402 under the pumping action that flows back (in figure not
Show) through reflux line 25, a part of methanol and DME are delivered to methanol distillation column 401 and flowed back, another part is through conveying
Pipeline 26 returns to DME reactors.The light component fixed gas that methanol distillation column return tank 402 obtains is through light component fixed gas delivery pipe
Road 23 is recycled back to MTP reactors.After the separating obtained technique water cooling of methanol distillation column 401 through process water conveyance conduit 24 send to
Subsequent oxide extraction unit (not shown).
Piece-rate system and method using the present invention in production practice are detached by hydrocarbon-water separative element 100, oil-gas
The multi-stage separation unit of unit 200, process water production unit 300 and methanol recovery unit 400 combines the piece-rate system to be formed, energy
Methanol to propylene reaction product (MTP reaction products) is kept completely separate with reaction water, process water effectively, MTP is reacted
Device outlet streams are more thoroughly separated into oil, water and gas, have ensured the smooth stable operation of subsequent gases compressibility,
And avoid the drying of follow-up hydrocarbon product there are larger difficulty, while also having ensured the long period even running of MTP process units, it keeps away
Exempt to cause to jump vehicle accident.The features such as separation method of the present invention has simple and reliable process, and stability is good.
The piece-rate system of the present invention is piece-rate system (such as the side in CN102363084A developed before this in the applicant
Case) on the basis of the improvement project that is carried out.The piece-rate system of the present invention, to the gas of MTP reaction products gained in separation process
The further separation of state hydrocarbon, the chilled water (chw) isolated to chilling system are further separated out hydrocarbon component and unreacted methanol
And dimethyl ether, it recycles；The water isolated further passes through 303 turns of process steam generator 302 and process steam knockout drum
The process steam for not carrying the drop containing salt secretly is turned to, efficiently avoids bringing alkali metal into MTP reactors and causes catalyst fast
Speed inactivation.This piece-rate system of the present invention, compared to pervious piece-rate system, in separating obtained oil gas, moisture is more
It is low, 100ppm is decreased below more than 500ppm by pervious, oil gas drying device switching frequency is reduced, extends drier
Replace the frequency.In addition, not carrying the process steam of alkali metal secretly by reducing entrainment water and production in oil gas, production dress has been ensured
Set macrocyclic even running.Technology is transformed existing commercial plant through the invention, works well after coming into operation, and device is real
Existing long-term operation, do not occur because oil gas entrainment water is high or process steam entrainment alkali metal ion is exceeded that device is caused to stop
Vehicle.
It will be understood by those skilled in the art that under the introduction of this specification, the present invention can be made some modifications or
Adjustment.These modifications or adjustment should also be as within the scope of the claims in the present invention.
Claims (10)
1. a kind of oil-water-gas separating system for process for preparing propylene from methanol, which is characterized in that including hydrocarbon-water separative element,
Oil-gas separative element, process steam production unit and methanol recovery unit；
The hydrocarbon-water separative element is for detaching the logistics of reaction product containing MTP and dilution steam generation, to obtain gaseous state
Hydrocarbon, heavy hydrocarbon component and the condensed water for having detached heavy hydrocarbon component；
The oil-gas separative element is used for folded in the gaseous hydrocarbon and heavy hydrocarbon component separating obtained to the hydrocarbon-water separative element
The water of band is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；
The process steam production unit is weighed at least partly described detached separating obtained to the hydrocarbon-water separative element
The condensed water of the hydrocarbon component is stripped, and to extract the water that hydrocarbon component therein and obtaining has extracted hydrocarbon component, is additionally operable to
The water for having extracted hydrocarbon component is handled to obtain the process steam for having detached the drop containing salt；
The methanol recovery unit at least partly described has detached heavy hydrocarbon group for separating obtained to the hydrocarbon-water separative element
The condensed water divided is handled, to isolate methanol contained therein, DME and light component fixed gas.
2. oil-water-gas separating system according to claim 1 for process for preparing propylene from methanol, which is characterized in that described
Hydrocarbon-water separative element includes pre- chilling tower, chilling tower and chilling water separation tank；
Wherein, the pre- chilling tower is equipped with the first entrance for inputting chilled water (chw) and lye, is additionally provided with anti-containing MTP for inputting
The second entrance of the logistics of product and dilution steam generation, the first entrance is answered to be located above the second entrance, the pre- chilling
Tower is for contacting the logistics of the reaction product containing MTP and dilution steam generation with chilled water (chw) and lye, reacted containing MTP described
The logistics of product and dilution steam generation is cooled down and is washed, and gaseous stream, heavy hydrocarbon component and condensed water are obtained；
The chilling tower is equipped with the third entrance for inputting chilled water (chw) and lye, is additionally provided with and comes from the pre- chilling for inputting
4th entrance of the gaseous stream of tower, the third entrance are located at the 4th entrance top, and the chilling tower will be for that will come from
The gaseous stream of the pre- chilling tower is contacted with chilled water (chw) and lye, the gaseous stream is cooled down and be washed, is obtained
Gaseous hydrocarbon, heavy hydrocarbon component and condensed water；
The chilling water separation tank is connected to by condensed water conveyance conduit respectively with pre- chilling tower, chilling tower, the chilling moisture
From tank for receive the condensed water from the pre- chilling tower and chilling tower and to remaining heavy hydrocarbon component in the condensed water into
Row separation, with the condensed water for obtaining heavy hydrocarbon component He having detached heavy hydrocarbon component；
Preferably, the chilling water separation tank passes through chilling respectively with the first entrance of pre- chilling tower, the third entrance of chilling tower
Water circulating pipe is connected to, at least partly described condensed water for having detached heavy hydrocarbon component for obtaining chilling water separation tank as
Chilled water (chw) is recycled to the pre- chilling tower and chilling tower respectively.
3. oil-water-gas separating system according to claim 2 for process for preparing propylene from methanol, which is characterized in that described
Oil-gas separative element includes compressor buffer tank, compressor and catch pot；
Wherein, it is connected to by gaseous hydrocarbon conveyance conduit between the compressor buffer tank and the chilling tower, the compressor is slow
Tank is rushed for being detached to the water carried secretly in the gaseous hydrocarbon from the chilling tower, to obtain liquid material and detach entrainment
Water gaseous hydrocarbon；Preferably, liquid material conveyance conduit is also associated between the compressor buffer tank and chilling tower, it will
The liquid material that the compressor buffer tank separation obtains is recycled to chilling tower；
The compressor is connected to the compressor buffer tank, and the compressor is for receiving compressor buffer tank separation institute
The gaseous hydrocarbon of the water for having detached entrainment obtained, and it is compressed and is cooled down to obtain gas mixture；
The catch pot is connected to the compressor by gas mixture conveyance conduit, the catch pot with it is described
Pre- chilling tower, chilling tower and chilling water separation tank are connected to by heavy hydrocarbon component conveyance conduit respectively, and the catch pot is used for
To the gas mixture from the compressor and the heavy hydrocarbon component from the pre- chilling tower, chilling tower and chilling water separation tank
The water of middle entrainment is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；Preferably, the catch pot and pressure
It is connected to by residual water conveyance conduit between contracting machine surge tank, for the remaining water to be fed through compressor buffer tank.
4. being used for oil-water-gas separating system of process for preparing propylene from methanol, feature according to claim 2-3 any one of them
It is, the process steam production unit includes process water extraction tower, process steam generator and process steam knockout drum；
Wherein, the process water extraction tower is connected to chilling water separation tank by the first chilled water (chw) conveyance conduit, and described first is anxious
Cold water conveyance conduit is for at least partly described condensed water for having detached heavy hydrocarbon component obtained by chilling water separation tank to be input to
Process water extraction tower；The process water extraction tower is equipped with the process steam input port for inputting process steam, the process water
The condensed water for having detached heavy hydrocarbon component that extraction tower is used to be inputted by the first chilled water (chw) conveyance conduit is steamed with technique
Vapour is contacted to extract remaining hydrocarbon component, and obtains the water for having extracted hydrocarbon component；Preferably, the process water extraction tower
It is connected to by hydrocarbon component conveyance conduit between pre- chilling tower, the hydrocarbon component for being extracted process water extraction tower follows
Ring is to pre- chilling tower；
The process steam generator passes through with the process water extraction tower for conveying the water for having extracted hydrocarbon component
Conveyance conduit is connected to, and the process steam generator is used to convert the water for having extracted hydrocarbon component to steam；
The process steam knockout drum is connected to the process steam generator by steam conveying pipe, the process steam point
It is used to detach the drop containing salt of entrained in the steam inputted by the steam conveying pipe from tank, to obtain process steam；
Preferably, demister is equipped in the process steam knockout drum；
The process steam input port of the process steam knockout drum and the process water extraction tower passes through process steam conveyance conduit
Connection, process water extraction tower is fed through by at least partly process steam obtained by process steam knockout drum.
5. oil-water-gas separating system according to claim 4 for process for preparing propylene from methanol, which is characterized in that described
Methanol recovery unit includes methanol distillation column and methanol distillation column return tank；
Wherein, the methanol distillation column is connected to the chilling water separation tank by the second chilled water (chw) conveyance conduit, and described second
Chilled water (chw) conveyance conduit is used to input at least partly described condensed water for having detached heavy hydrocarbon component obtained by chilling water separation tank
To methanol distillation column, the methanol distillation column is used to carry out essence to inputting the condensed water for having detached heavy hydrocarbon component therein
It evaporates, to obtain process water and the liquid phase component containing methanol and DME；Preferably, the methanol distillation column and the process steam
Generator is connected to by sewage running piping, and the sewage running piping is used to convey the sewage of process steam generator discharge,
The methanol distillation column is additionally operable to receive the sewage conveyed by the sewage running piping and carries out rectifying to it, to obtain
Process water and liquid phase component containing methanol and DME；
The methanol distillation column return tank is connected to the methanol distillation column by liquid phase component conveyance conduit, the Methanol Recovery
Tower return tank is used to detach to inputting liquid phase component therein, to obtain methanol, DME and light component fixed gas；
Preferably, reflux line, the return duct are connected between the methanol distillation column return tank and the methanol distillation column
Road is used at least partly methanol and DME that methanol distillation column return tank separation obtains being back to the methanol distillation column.
6. it is a kind of using claim 1-5 any one of them piece-rate system to the oil-in process for preparing propylene from methanol products therefrom
The method that water-gas is detached, which is characterized in that the method includes：
The logistics of reaction product containing MTP and dilution steam generation is detached using the hydrocarbon-water separative element, to obtain gaseous state
Hydrocarbon, heavy hydrocarbon component and the condensed water for having detached heavy hydrocarbon component；
Folded by the oil-gas separative element gaseous hydrocarbon and heavy hydrocarbon component separating obtained to the hydrocarbon-water separative element
The water of band is detached, to obtain gaseous component, hydrocarbon lime set and remaining water；
It is weighed using the process steam production unit at least partly described detached separating obtained to the hydrocarbon-water separative element
The condensed water of the hydrocarbon component is stripped, to isolate wherein remaining hydrocarbon component；And the water that the hydrocarbon component will have been extracted
It is handled, isolates the drop containing salt wherein carried secretly, obtain process steam；
Heavy hydrocarbon group has been detached using at least partly described separating obtained to the hydrocarbon-water separative element of the methanol recovery unit
The condensed water divided is handled, and separation obtains methanol, DME and light component fixed gas.
7. according to the method described in claim 6, it is characterized in that, the hydrocarbon-water separative element includes pre- chilling tower, chilling tower
With chilling water separation tank；The pre- chilling tower is equipped with first entrance and second entrance, and the first entrance enters positioned at described second
Above mouthful；The chilling tower is equipped with third entrance and the 4th entrance, and the third entrance is located at the 4th entrance top, described
Method includes：
The logistics of reaction product containing MTP and dilution steam generation is fed through pre- chilling tower by the second entrance, by chilled water (chw) and alkali
Liquid is fed through pre- chilling tower by the first entrance, and the logistics of the reaction product containing MTP and dilution steam generation enters pre- chilling tower
Afterwards, being contacted with chilled water (chw) and lye and be able to cool down and wash from bottom to top, obtains gaseous stream, heavy hydrocarbon component and condensed water；
The gaseous stream that pre- chilling tower obtains is fed through chilling tower via the 4th entrance, by chilled water (chw) and lye by described
Third entrance is fed through chilling tower, and the gaseous stream enters after chilling tower contacting and be able to chilled water (chw) and lye from bottom to top
Cooling and washing, obtain gaseous hydrocarbon, heavy hydrocarbon component and condensed water；
Condensed water obtained by the pre- chilling tower and chilling tower is fed through chilling water separation tank, is isolated remaining in condensed water
Heavy hydrocarbon component, and obtain the condensed water for having detached heavy hydrocarbon component；
Preferably, at least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is as chilled water (chw)
It is recycled to the pre- chilling tower and chilling tower；
Preferably, the logistics of the reaction product containing MTP and dilution steam generation carries out heat time before being sent into the pre- chilling tower
It receives, and its temperature is controlled at 170-210 DEG C；
Preferably, the temperature of chilled water (chw) used in the pre- chilling tower and lye is 48-52 DEG C；It is fed through the chilling tower
The temperature of gaseous stream from the pre- chilling tower is 50-60 DEG C；The temperature of chilled water (chw) and lye used in the chilling tower
Degree is 38-42 DEG C.
8. the method according to the description of claim 7 is characterized in that the oil-gas separative element includes compressor buffer tank, pressure
Contracting machine and catch pot；The method includes：
The separating obtained gaseous hydrocarbon of the chilling tower is fed through compressor buffer tank, isolates and is carried secretly in the gaseous hydrocarbon
Water obtains liquid material and has detached the gaseous hydrocarbon of the water of entrainment；Preferably, the liquid material is fed through in chilling tower；
The gaseous hydrocarbon of the water for having detached entrainment obtained by the compressor buffer tank is fed through compressor, through compressor pressure
After contracting and cooling, gas mixture is obtained；
The gas mixture and the pre- chilling tower, chilling tower and chilling water separation tank that the compressor is obtained are isolated
Heavy hydrocarbon component is fed through catch pot, isolates the water wherein carried secretly, obtains gaseous component, hydrocarbon lime set and remaining water；
Preferably, the remaining water is fed through compressor buffer tank.
9. method according to claim 7 or 8, which is characterized in that the process steam production unit includes that process water is taken out
Stripper, process steam generator and process steam knockout drum；The method includes：
At least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is fed through the technique
Water extraction tower inputs process steam into process water extraction tower, using the process steam to described in process water extraction tower
The condensed water for having detached heavy hydrocarbon component is stripped, and to isolate wherein remaining hydrocarbon component, obtains hydrocarbon component and extracting
The water of hydrocarbon component；Preferably, the separating obtained hydrocarbon component of the process water extraction tower is recycled to pre- chilling tower；It is preferred that
, at least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is entering process water pumping
It before stripper, is pressurizeed, and is filtered to detach particulate matter therein using chilling water pump；
The water for having extracted hydrocarbon component obtained by process water extraction tower is fed through process steam generator, obtains steam；
Preferably, the water for having extracted hydrocarbon component is pressurizeed and is preheated, preferably before being sent into the process steam generator
It is preheated to 140-150 DEG C；
The steam that the process steam generator generates is fed through process steam knockout drum, isolates the saliferous carried secretly in steam
Class drop obtains process steam；
At least partly process steam that the process steam generator obtains is input to process water extraction tower.
10. according to the method described in claim 9, it is characterized in that, the methanol recovery unit includes methanol distillation column and first
Alcohol recovery tower return tank；The method includes：
At least partly described condensed water for having detached heavy hydrocarbon component that the chilling water separation tank obtains is fed through Methanol Recovery
Tower detaches through rectifying and obtains process water and the liquid phase component containing methanol and DME；Preferably, also the process steam is occurred
The sewage of device discharge is fed through the methanol distillation column and carries out rectifying, to obtain process water and the liquid phase containing methanol and DME；
The liquid phase component obtained by methanol distillation column is fed through methanol distillation column return tank, separation obtains methanol, DME and light
Component fixed gas；Separating obtained at least partly methanol and DME are back to the methanol distillation column.
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| EP3712125A1 (en) * | 2019-03-22 | 2020-09-23 | L'air Liquide, Société Anonyme Pour L'Étude Et L'exploitation Des Procédés Georges Claude | Quench system and method for quenching a product flow |
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