CN110950733B - Separation device and method for preparing olefin gas from methanol - Google Patents
Separation device and method for preparing olefin gas from methanol Download PDFInfo
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- CN110950733B CN110950733B CN201811130571.1A CN201811130571A CN110950733B CN 110950733 B CN110950733 B CN 110950733B CN 201811130571 A CN201811130571 A CN 201811130571A CN 110950733 B CN110950733 B CN 110950733B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
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- 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
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention discloses a separation device and a method for methanol-to-olefin gas, wherein after pretreatment is carried out on the methanol-to-olefin gas through a pretreatment component (1), the methanol-to-olefin gas is subjected to phase separation in a separator (2), condensate is sent to a condensate dryer (3), gas phase is sent to a first gas phase dryer (4), all the gas phase is sent to a deethanizer (5) after being dried, gas phase at the top of the deethanizer (5) is separated by a demethanizer (6), a solvent recovery tower (7), an acetylene converter (8) and an ethylene rectifying tower (9) to obtain ethylene, and the bottom of the deethanizer (5) is separated by a depropanizer (10) and a propylene rectifying tower (11) to obtain propylene. The circulation loop of the absorbent is a demethanizer (6) -a solvent recovery tower (7) -a demethanizer (6), the circulation loop is short, the deethanizer (5) and the propylene rectifying tower (11) are not involved, and the loads, the energy consumption and the equipment investment of the deethanizer (5) and the propylene rectifying tower (11) are effectively reduced.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a separation device and a separation method for preparing olefin gas from methanol.
Background
In recent years, although olefin production at home and abroad has been a trend of diversification, a non-steam cracking hydrocarbon production method represented by Methanol To Olefin (MTO) is still an important method for producing olefins. The preparation of olefin from methanol is a chemical process technology for producing low-carbon olefin by using methanol synthesized by coal or natural gas as a raw material and adopting a fluidized bed reaction form similar to a catalytic cracking device, and the main products are ethylene, propylene and the like.
The most widely used separation scheme for MTO gas is the lumes front-end depropanization process. In the process, the reaction gas enters a depropanizer from an MTO reactor, and the substrate of the depropanizer flows into a debutanizer to separate mixed C 4 Component, the top material of the depropanizer is flowed through the demethanizer to remove H component and C component 1 The components are sent to a deethanizer, the top material flow of the deethanizer is sent to an ethylene rectifying tower to separate ethylene, and the bottom material flow of the deethanizer is sent to a propylene rectifying tower to separate propylene. The process is characterized in that: propylene is taken as a refrigerant, the top of the demethanizer is utilized to absorb the medium-cooling oil, and the bottom C of the partial deethanizer is adopted 3 The distillate and the bottom propane of the propylene rectifying tower are used as absorbent to reduce ethylene loss.
In carrying out the invention, the present inventors have found that there are at least the following problems in the prior art:
because the top of the demethanizer in the gas separation process of the prior art utilizes an intercooling oil absorption method, the bottom C of the partial deethanizer is adopted 3 The fraction and the propylene rectifying tower bottom propane are used as absorbent to recover ethylene, and the absorbent is separated from the demethanizer tower bottom and then sent to the deethanizer, separated from the deethanizer tower bottom and sent to the propylene rectifying tower, and finally sent from the propylene rectifying tower bottomThe separated absorber is returned to the top of the demethanizer, that is, the circulation loop of the absorber is a demethanizer-deethanizer-propylene rectifying tower-demethanizer, and the circulation loop is long, so that the loads and the energy consumption of the demethanizer, the deethanizer and the propylene rectifying tower are increased, and the operation of a separation unit in the circulation loop is easy to be unstable.
Disclosure of Invention
In view of this, the invention provides a separation device and a separation method for methanol-to-olefin gas, which solve the problem of long absorber circulation loop in the prior art and reduce the load, energy consumption and equipment investment of a deethanizer and a propylene rectifying tower.
Specifically, the method comprises the following technical scheme:
in one aspect, an embodiment of the present invention provides a separation apparatus for methanol-to-olefin gas, the apparatus comprising: a pretreatment assembly, a separator, a condensate dryer, a first gas phase dryer, a deethanizer, a demethanizer, a solvent recovery tower, an acetylene converter, an ethylene rectification tower, a depropanizer, a propylene rectification tower and a debutanizer, wherein,
the pretreatment component is communicated with an inlet of the separator, a gas phase outlet of the separator is communicated with an inlet of the first gas phase dryer, a condensate outlet of the separator is communicated with an inlet of the condensate dryer, the condensate dryer is communicated with a liquid phase inlet of the deethanizer, an outlet of the first gas phase dryer is communicated with the gas phase inlet of the deethanizer, a tower top outlet of the deethanizer is communicated with a tower body inlet of the demethanizer, and a tower top outlet of the demethanizer is communicated with a fuel gas collector;
the bottom outlet of the demethanizer is communicated with the inlet of the solvent recovery tower, the bottom outlet of the solvent recovery tower is communicated with the top inlet of the demethanizer, the top outlet of the solvent recovery tower is communicated with the inlet of the acetylene converter, the outlet of the acetylene converter is communicated with the inlet of the ethylene rectification tower, the top outlet of the ethylene rectification tower is communicated with an ethylene collector, and the bottom outlet of the ethylene rectification tower is communicated with an ethane collector;
the bottom outlet of the deethanizer is communicated with the inlet of the depropanizer, the top outlet of the depropanizer is communicated with the inlet of the propylene rectifying tower, the top outlet of the propylene rectifying tower is communicated with the propylene collector, and the bottom outlet of the propylene rectifying tower is communicated with the propane collector;
the bottom outlet of the depropanizer is communicated with the inlet of the debutanizer, the top outlet of the debutanizer is communicated with a C4 component collector, and the bottom outlet of the debutanizer is communicated with a C5 and above component collector.
Optionally, the pretreatment component comprises a quenching tower, a water stripping tower, a methanol recovery tower, a first compressor section, a second compressor section, a water washing tower, a third compressor section, an alkaline washing tower and a waste lye pretreatment tower;
the inlet of the quenching tower is communicated with the methanol-to-olefin reactor, the outlet of the top of the quenching tower is communicated with the inlet of the methanol recovery tower, the outlet of the top of the methanol recovery tower is communicated with the inlet of the first section of the compressor, the outlet of the first section of the compressor is communicated with the inlet of the second section of the compressor, the outlet of the second section of the compressor is communicated with the inlet of the water scrubber, the outlet of the water scrubber is communicated with the inlet of the third section of the compressor, the outlet of the third section of the compressor is communicated with the inlet of the caustic scrubber, and the outlet of the top of the caustic scrubber is communicated with the inlet of the separator;
the outlet of the bottom of the alkali washing tower is communicated with the inlet of the waste alkali liquor pretreatment tower, and the outlet of the waste alkali liquor pretreatment tower is communicated with a waste alkali liquor collector;
the bottom outlet of the quenching tower is communicated with the inlet of the water stripping tower, the bottom outlet of the methanol recovery tower is communicated with the inlet of the water stripping tower, and the outlet of the water stripping tower is communicated with a water collector;
optionally, the depropanizer comprises a high pressure depropanizer and a low pressure depropanizer;
the bottom outlet of the deethanizer is communicated with the inlet of the high-pressure depropanizer, and the top outlet of the high-pressure depropanizer is communicated with the inlet of the propylene rectifying tower;
the bottom outlet of the high-pressure depropanizer is communicated with the inlet of the low-pressure depropanizer, and the bottom outlet of the low-pressure depropanizer is communicated with the inlet of the debutanizer.
Optionally, the apparatus further comprises: a heat exchanger;
the bottom outlet of the high-pressure depropanizer is communicated with the inlet of the low-pressure depropanizer through the heat exchanger;
and the outlet of the top of the low-pressure depropanizer is communicated with the inlet of the high-pressure depropanizer through the heat exchanger.
Optionally, the propylene rectification tower comprises a first propylene rectification tower and a second propylene rectification tower;
the top outlet of the high-pressure depropanizer is communicated with the inlet of the first propylene rectifying tower, and the top outlet of the first propylene rectifying tower is communicated with the propylene collector;
the bottom outlet of the first propylene rectifying tower is communicated with the inlet of the second propylene rectifying tower, and the bottom outlet of the second propylene rectifying tower is communicated with the propane collector;
the top outlet of the second propylene rectifying tower is communicated with the inlet of the first propylene rectifying tower.
Optionally, the apparatus further comprises: a compressor four-stage;
the compressor four stages are disposed between the deethanizer and the demethanizer.
Optionally, the apparatus further comprises: a second gas phase dryer;
the second gas phase dryer is disposed between the acetylene converter and the ethylene rectification column.
Optionally, a middle boiler and a reboiler are arranged in the ethylene rectifying tower;
the middle boiler is arranged at 80-110 layers of theoretical plates from the top of the tower to the bottom of the ethylene rectifying tower;
the reboiler is arranged at the bottom of the ethylene rectifying tower.
Optionally, the 2 nd-10 th layer theoretical plates from the top of the ethylene rectifying tower to the bottom of the tower are provided with side lines, and the side lines are communicated with the ethylene collector.
On the other hand, the embodiment of the invention also provides a separation method of the methanol-to-olefin gas, which comprises the following steps:
pretreating a reaction product of a reactor for preparing olefin from methanol, and then sending the pretreated reaction product into a separator for gas-liquid separation to obtain a gas-phase product and a condensate product;
the gas phase product is sent into a first gas phase dryer for drying and then is sent into a deethanizer to obtain components with C2 and less than C2 at the top of the tower and components with C3 and more than C3 at the bottom of the tower;
sending the components with the C2 and below C2 and the absorbent at the top of the tower to a demethanizer to obtain a mixture of fuel gas at the top of the tower, the C2 component at the bottom of the tower and the absorbent;
feeding the mixture of the C2 component and the absorbent at the bottom of the tower to a solvent recovery tower to obtain the C2 component at the top of the tower and the absorbent at the bottom of the tower, and feeding the absorbent at the bottom of the tower back to the demethanizer again;
sending the C2 component at the top of the tower into an acetylene converter for conversion, and then sending the converted C2 component into an ethylene rectifying tower to obtain ethylene at the top of the tower and ethane at the bottom of the tower;
sending the components with the C3 and above C3 at the bottom of the tower into a depropanizer to obtain the C3 component at the top of the tower and the components with the C4 and above C4 at the bottom of the tower;
sending the C3 component at the top of the tower into a propylene rectifying tower to obtain propylene at the top of the tower and propane at the bottom of the tower;
and sending the components with the C4 level more than C4 at the bottom of the tower to a debutanizer to obtain the C4 components at the top of the tower and the components with the C5 level more than C5 at the bottom of the tower.
Alternatively, the absorbent is propane.
Alternatively, the deethanizer has a column top gauge pressure of 1.6-2.2MPa and a column top temperature of-30-39deg.C.
Optionally, the top gauge pressure of the demethanizer is 2.5-3.5MPa, and the top temperature is-30-39 ℃.
Optionally, the top gauge pressure of the solvent recovery tower is 2.0-3.0MPa, and the top temperature is-10-30 ℃.
Optionally, the top gauge pressure of the ethylene rectifying tower is 1.0-2.0MPa, and the top temperature is-30-39 ℃.
The technical scheme provided by the embodiment of the invention has the beneficial effects that at least:
1. after pretreatment of the methanol-to-olefin gas through a pretreatment component, carrying out phase separation in a separator, sending condensate to a condensate dryer, sending gas phase to a first gas-phase dryer, drying and sending the gas phase to a deethanizer, separating the gas phase at the top of the deethanizer by a demethanizer, a solvent recovery tower, an acetylene converter and an ethylene rectifying tower to obtain ethylene, and separating the bottom of the deethanizer by a depropanizer and a propylene rectifying tower to obtain propylene, thereby realizing separation of the methanol-to-olefin gas;
2. through setting up the solvent recovery tower, when the absorbent that uses in the demethanizer can mix with the C2 component of tower bottom and enter into the solvent recovery tower, C2 component and absorbent separate in the solvent recovery tower, obtain the absorbent at the top of the tower, and the absorbent at the bottom of the tower can flow back to the demethanizer from the solvent recovery tower again after cooling down, realized the cyclic utilization of absorbent, the circulation loop of this absorbent is demethanizer-solvent recovery tower-demethanizer, this circulation loop is short, and do not involve deethanizer and propylene rectifying column, can effectively reduce load, energy consumption and the equipment investment of deethanizer and propylene rectifying column.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic structural diagram of a separation device for producing olefin gas from methanol according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of another separation device for producing olefin gas from methanol according to an embodiment of the present invention;
fig. 3 is a flow chart of a method for separating a methanol-to-olefin gas according to an embodiment of the present invention.
Reference numerals in the drawings are respectively expressed as:
1-pretreatment component, 101-quench tower, 102-water stripper, 103-methanol recovery tower, 104-first compressor section, 105-second compressor section, 106-water scrubber, 107-third compressor section, 108-alkaline scrubber, 109-waste lye pretreatment tower,
a 2-separator, wherein the separator is provided with a plurality of separation chambers,
a 3-condensate dryer which comprises a water tank and a water tank,
4-a first gas-phase dryer, in which the first gas-phase dryer,
a 5-deethanizer column, wherein the catalyst is a catalyst,
a 6-demethanizer column, which is provided with a bottom,
7-a solvent recovery tower, wherein the solvent recovery tower is provided with a plurality of solvent recovery towers,
an 8-acetylene converter, wherein the energy of the gas is converted into oxygen,
a 9-ethylene rectifying tower,
10-depropanizer, 1001-high pressure depropanizer, 1002-low pressure depropanizer,
11-propylene rectifying tower, 1101-first propylene rectifying tower, 1102-second propylene rectifying tower,
a 12-debutanizer column, wherein the two ends of the column are connected with a water inlet of a water inlet pipe of a water outlet pipe of a,
13-a fuel gas collector, wherein the fuel gas collector is arranged on the fuel gas collector,
a 14-ethylene collector, wherein the ethylene collector,
a 15-ethane collector, which is connected with the gas-liquid separator,
a 16-propylene collector, which comprises a gas-liquid separator,
a 17-propane collector, wherein the collector comprises a bottom plate,
an 18-C4 component collector,
19-C5 and above C5 component collector,
a reactor for preparing olefin from 20-methanol,
21-a waste lye collector,
a 22-water collector, which is connected with the water collector,
a 23-heat exchanger, wherein the heat exchanger is provided with a heat-exchanging pipe,
a four-stage compressor with a four-stage compressor,
25-a second gas phase dryer.
Detailed Description
Unless defined otherwise, all technical terms used in the embodiments of the present invention have the same meaning as commonly understood by one of ordinary skill in the art. For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, the embodiments of the present invention will be described in further detail with reference to the accompanying drawings.
In a first aspect, an embodiment of the present invention provides a separation apparatus for producing an olefin gas from methanol, as shown in fig. 1, where the apparatus includes: a pretreatment module 1, a separator 2, a condensate dryer 3, a first gas phase dryer 4, a deethanizer 5, a demethanizer 6, a solvent recovery column 7, an acetylene converter 8, an ethylene rectification column 9, a depropanizer 10, a propylene rectification column 11, and a debutanizer 12.
Wherein the pretreatment assembly 1 is communicated with an inlet of the separator 2, a gas phase outlet of the separator 2 is communicated with an inlet of the first gas phase dryer 4, a condensate outlet of the separator 2 is communicated with an inlet of the condensate dryer 3, an outlet of the condensate dryer 3 is communicated with a liquid phase inlet of the deethanizer 5, an outlet of the first gas phase dryer 4 is communicated with a gas phase inlet of the deethanizer 5, a tower top outlet of the deethanizer 5 is communicated with a tower body inlet of the demethanizer 6, and a tower top outlet of the demethanizer 6 is communicated with the fuel gas collector 13;
the bottom outlet of the demethanizer 6 is communicated with the inlet of the solvent recovery tower 7, the bottom outlet of the solvent recovery tower 7 is communicated with the top inlet of the demethanizer 6, the top outlet of the solvent recovery tower 7 is communicated with the inlet of the acetylene converter 8, the outlet of the acetylene converter 8 is communicated with the inlet of the ethylene rectifying tower 9, the top outlet of the ethylene rectifying tower 9 is communicated with the ethylene collector 14, and the bottom outlet of the ethylene rectifying tower 9 is communicated with the ethane collector 15;
the bottom outlet of the deethanizer 5 is communicated with the inlet of the depropanizer 10, the top outlet of the depropanizer 10 is communicated with the inlet of the propylene rectifying tower 11, the top outlet of the propylene rectifying tower 11 is communicated with the propylene collector 16, and the bottom outlet of the propylene rectifying tower 11 is communicated with the propane collector 17;
the bottom outlet of the depropanizer 10 is in communication with the inlet of the debutanizer 12, the top outlet of the debutanizer 12 is in communication with the C4 components collector 18, and the bottom outlet of the debutanizer 12 is in communication with the C5 and above components collector 19.
It will be appreciated that the components within the device are in communication with each other via tubing.
The ethylene obtained in the ethylene rectifying column 9 was polymer grade ethylene, and the propylene obtained in the propylene rectifying column 11 was polymer grade propylene.
The following describes the working principle of the separation device for methanol-to-olefin gas according to the embodiment of the present invention:
the olefin mixed gas obtained by the reaction in the reactor 20 for preparing olefin from methanol is pretreated and then enters a separator 2 for gas-liquid separation to obtain a gas phase component and a condensate component;
the gas phase component enters a first gas phase dryer 4 from an upper outlet of a separator 2 for drying gas, and then enters a deethanizer 5 to obtain components with C2 and less than C2 at the top of the tower and components with C3 and more than C3 at the bottom of the tower; the components with C2 and below C2 at the top of the tower enter a demethanizer 6 from the top outlet of the deethanizer 5, an absorbent is added while the components with C2 and below C2 are injected into the demethanizer 6, methane is removed by an intercooled oil absorption method, fuel gas (hydrogen and methane) is obtained at the top of the demethanizer 6, and is collected by a fuel gas collector 13, and a mixture of the C2 component and the absorbent is obtained at the bottom of the demethanizer 6;
the mixture of the C2 component and the absorbent at the bottom of the demethanizer 6 flows out from the bottom outlet of the demethanizer 6, enters the solvent recovery tower 7, the C2 component and the absorbent are separated in the solvent recovery tower 7, the absorbent returns to the demethanizer 6 after being cooled at the bottom of the solvent recovery tower 7, enters the demethanizer 6 from the top inlet of the demethanizer 6, and methane is continuously removed by using an intercooler oil absorption method, so that recycling of the absorbent is realized;
the C2 component obtained from the top of the solvent recovery tower 7 enters an acetylene converter 8 for hydrotreating, then enters an ethylene rectifying tower 9, ethylene is separated, ethylene is obtained from the top of the ethylene rectifying tower 9 and is collected by an ethylene collector 14, ethane is obtained from the bottom of the ethylene rectifying tower 9 and is collected by an ethane collector 15;
the C3 and above C3 components at the bottom of the deethanizer 5 enter a depropanizer 9 to obtain a C3 component at the top of the tower and a C4 and above C4 component at the bottom of the tower, the C3 component at the top of the tower enters a propylene rectifying tower 11, propylene separated from the top of the propylene rectifying tower 11 is obtained through the propylene rectifying tower 11 and is collected through a propylene collector 16, and propane separated from the bottom of the propylene rectifying tower 11 is obtained through a propane collector 17;
the C4 and above components obtained at the bottom of the depropanizer 9 are fed into the depropanizer, the C4 components are obtained from the top of the depropanizer 12 and collected by a C4 component collector 18, and the C5 and above components obtained from the bottom of the depropanizer 12 are collected by a C5 and above C5 component collector 19.
The cold oil absorption method mentioned here refers to the use of-40 ℃ propylene refrigerant refrigeration in combination with propane absorbent to reduce ethylene runaway.
It should be noted that, the absorbent may be one or more of C3, C4 or C5, preferably propane, to absorb ethylene by gas-liquid equilibrium principle, so as to improve the recovery rate of ethylene; the propylene refrigerant is provided with three temperature levels of 7 ℃, -24 ℃, -40 ℃.
Therefore, the separation device for the methanol-to-olefin gas utilizes the pretreatment component 1, the separator 2, the condensate dryer 3, the first gas phase dryer 4, the deethanizer 5, the demethanizer 6, the solvent recovery tower 7, the acetylene converter 8, the ethylene rectification tower 9, the depropanizer 10, the propylene rectification tower 11 and the debutanizer 12, realizes the separation of the methanol-to-olefin gas, changes the circulation loop of the absorbent used in the demethanizer 6 into the demethanizer 6-solvent recovery tower 7-demethanizer 6, shortens the circulation loop, does not involve the deethanizer 5 and the propylene rectification tower 11, can effectively reduce the load, the energy consumption and the equipment investment of the deethanizer 5 and the propylene rectification tower 11, and improves the stability of the device.
The structure of each part of the separation device for methanol-to-olefin gas in the embodiment of the invention is further described and illustrated below:
as for the pretreatment module 1, it plays a role of pretreatment of a mixed gas obtained by methanol to olefins, specifically, the pretreatment module 1 includes a quenching tower 101, a water stripper 102, a methanol recovery tower 103, a compressor one section 104, a compressor two section 105, a water scrubber 106, a compressor three section 107, an alkaline scrubber 108, and a spent lye pretreatment tower 109, as shown in fig. 2.
Wherein, the inlet of the quenching tower 101 is communicated with the methanol-to-olefin reactor 20, the outlet of the top of the quenching tower 101 is communicated with the inlet of the methanol recovery tower 103, the outlet of the top of the methanol recovery tower 103 is communicated with the inlet of the first section 104 of the compressor, the outlet of the first section 104 of the compressor is communicated with the inlet of the second section 105 of the compressor, the outlet of the second section 105 of the compressor is communicated with the inlet of the water washing tower 106, the outlet of the water washing tower 106 is communicated with the inlet of the third section 107 of the compressor, the outlet of the third section 107 of the compressor is communicated with the inlet of the alkaline washing tower 108, and the outlet of the top of the alkaline washing tower 108 is communicated with the inlet of the separator 2;
the bottom outlet of the alkali washing tower 108 is communicated with the inlet of the waste alkali pretreatment tower 109, and the outlet of the waste alkali pretreatment tower 109 is communicated with the waste alkali collector 21;
the bottom outlet of the quenching tower 101 is communicated with the inlet of the water stripper 102, the bottom outlet of the methanol recovery tower 103 is communicated with the inlet of the water stripper 102, and the outlet of the water stripper 102 is communicated with the water collector 22;
so arranged, after the mixed olefin gas obtained by the reaction in the reactor 20 for preparing olefin from methanol enters the quenching tower 101 for heat recovery, the mixed olefin gas enters the methanol recovery tower 103 from the top outlet of the quenching tower 101 for recovering methanol, then enters the water scrubber 106 for washing after being compressed by the first section 104 and the second section 105 of the compressor for removing oxide impurities such as methanol, dimethyl ether and the like, and then enters the alkaline scrubber 108 for removing acid gases such as carbon dioxide after being compressed again by the third section 107 of the compressor;
the waste lye in the alkali washing tower 108 enters the waste lye pretreatment tower 109 through the tower bottom outlet of the alkali washing tower 108, and is collected into a waste lye collector 21 for subsequent treatment or use after being pretreated by the waste lye pretreatment tower 109;
the liquid phase cooled by the quench tower 101 enters the water stripper 102 through the bottom outlet of the quench tower 101, and the water stripper 102 strips out hydrocarbon components in the water to obtain purified water, so that the outlet of the water stripper 102 can be communicated with the water collector 22 to collect the water.
It will be appreciated that after recovering methanol, the liquid phase component may be further recovered by the methanol recovery column 103, and purified water may be obtained by communicating the bottom outlet of the methanol recovery column 103 with the inlet of the water stripper 102.
The gas after cooling, compression, water washing and alkali washing is the pretreated gas, and can be further separated.
For separator 2, separator 2 serves to separate the components of each phase, in the present embodiment separator 2 is a gas-liquid-water three-phase separator.
For the depropanizer 10, the depropanizer 10 functions to separate C3 from C4 and above components, specifically, the depropanizer 10 includes a high pressure depropanizer 1001 and a low pressure depropanizer 1002, as shown in fig. 2.
Wherein the bottom outlet of the deethanizer 5 is communicated with the inlet of the high-pressure depropanizer 1001, and the top outlet of the high-pressure depropanizer 1001 is communicated with the inlet of the propylene rectifying tower 11;
the bottom outlet of the high pressure depropanizer 1001 is in communication with the inlet of the low pressure depropanizer 1002 and the bottom outlet of the low pressure depropanizer 1002 is in communication with the inlet of the debutanizer 12.
By arranging the high-pressure depropanizer 1001 and the low-pressure depropanizer 1002, the temperature distribution and the refrigerant matching in the demethanizer 6 can be more reasonable; compared with the single depropanizer 10, the total load of the high-pressure depropanizer 1001 and the low-pressure depropanizer 1002 is lower, the tower top of the high-pressure depropanizer 1001 does not need liquid phase discharging, the low-pressure steam consumption in the tower bottom reboiler of the low-pressure depropanizer 1002 is obviously reduced, and the energy consumption can be saved to a certain extent; in addition, the combination of the high pressure depropanizer 1001 and the low pressure depropanizer 1002 can reduce the generation of polymers and fouling and blocking of tower plates in the depropanizer 10 by unsaturated hydrocarbons (such as butadiene) with more than 4 carbon atoms and more than 4 carbon atoms, so that the problems of reduced separation efficiency and increased separation load are solved, and the running period of the device can be prolonged.
Based on the high pressure depropanizer 1001 and the low pressure depropanizer 1002, the separation device for preparing olefin gas from methanol according to the embodiment of the present invention further includes: a heat exchanger 23.
Wherein the bottom outlet of the high pressure depropanizer 1001 is communicated with the inlet of the low pressure depropanizer 1002 via a heat exchanger 23; the overhead outlet of the low pressure depropanizer 1002 is in communication with the inlet of the high pressure depropanizer 1001 via heat exchanger 23 as shown in figure 2.
By providing the heat exchanger 23, the bottom hot stream of the high pressure depropanizer 1001 and the top cold stream of the low pressure depropanizer 1002 can exchange heat with each other to meet the process requirements in the respective columns.
For the propylene rectification tower 11, the propylene rectification tower 11 comprises a first propylene rectification tower 1101 and a second propylene rectification tower 1102 for better separation of propylene from propane.
Wherein the top outlet of the high pressure depropanizer 1001 is connected to the inlet of the first propylene rectifying tower 1101, and the top outlet of the first propylene rectifying tower 1101 is connected to the propylene collector 16;
the bottom outlet of the first propylene rectifying tower 1101 is communicated with the inlet of the second propylene rectifying tower 1102, and the bottom outlet of the second propylene rectifying tower 1102 is communicated with the propane collector 17;
the top outlet of the second propylene rectification tower 1102 is in communication with the inlet of the first propylene rectification tower 1101 as shown in figure 2.
By providing the first propylene rectifying column 1101 and the second propylene rectifying column 1102, the recovery rate of propylene can be improved after two times of rectification.
It will be appreciated that the propane obtained at the bottom of the second propylene rectification tower 1102 may be sent to the propane recovery stage 17 or to the solvent recovery tower 7 to make up for absorbent losses.
In order to better realize the removal of methane, the separation device of the methanol-to-olefin gas in the embodiment of the invention further comprises: compressor four stage 24, compressor four stage 24 is disposed between deethanizer 5 and demethanizer 6, as shown in fig. 2.
The C2 and C2-less components exiting the overhead outlet of deethanizer 5 may be compressed in four stages 24 of the compressor and then fed to demethanizer 6 for further demethanization.
In order to better separate ethylene and ethane, since the conversion is performed by the hydrotreatment in the acetylene converter 8, the recovery rate of ethylene is improved, and the separation apparatus of the methanol-to-olefin gas according to the embodiment of the present invention further includes: a second gas phase dryer 25;
a second gas phase dryer 25 is provided between the acetylene converter 8 and the ethylene rectification column 9 as shown in fig. 2.
The product water after conversion by the acetylene converter 8 can be removed by means of a second gas phase dryer 25.
In order to further reduce the energy consumption of the apparatus, in the embodiment of the present invention, a mid-boiler (not shown in the figure) and a reboiler (not shown in the figure) are provided in the ethylene rectification column 9.
Wherein, the middle boiler is arranged at 80-110 layers of theoretical plates from the top of the tower to the bottom of the ethylene rectifying tower 9, and the reboiler is arranged at the bottom of the ethylene rectifying tower 9.
By adopting the propylene refrigerant to supply heat in the middle boiler and the reboiler, the waste heat can be effectively recovered, the consumption of the propylene refrigerant is reduced, the power consumption of the propylene refrigeration compressor is reduced, and the reduction of the energy consumption of the device is further realized.
In order to collect ethylene more conveniently, the ethylene rectifying tower 9 is provided with a side line on the 2-10 layers of theoretical plates from the top to the bottom, and the side line is communicated with the ethylene collector 14, so that the ethylene can be collected.
In a second aspect, an embodiment of the present invention further provides a method for separating a gas for preparing olefins from methanol, where a flowchart of the method is shown in fig. 3, and the method includes:
step 301: the reaction product of the reactor 20 for preparing olefin from methanol is pretreated and then sent into a separator 2 for gas-liquid separation, thus obtaining gas phase product and condensate product.
Specifically, the pretreatment of the reaction product of the methanol-to-olefin reactor 20 mainly comprises the steps of feeding the reaction product into a quenching tower 101 and a methanol recovery tower 103 for heat recovery and methanol recovery, compressing the reaction product by a first compressor section 104 and a second compressor section 105, feeding the reaction product into a water scrubber 106 for removing oxide impurities, compressing the reaction product by a third compressor section 107, and feeding the reaction product into a caustic scrubber 108 for removing acid gas.
Wherein the separator 2 is a gas-liquid-water three-phase separator, and three phases can be separated in the separator 2.
Step 302: and respectively sending the condensate product and the gas-phase product into a condensate dryer 3 and a first gas-phase dryer 4 for drying, and then sending the condensate product and the gas-phase product into a deethanizer 5 to obtain components below C2 and C2 at the top of the tower and components above C3 and C3 at the bottom of the tower.
Specifically, in terms of the setting of pressure and temperature, the column top gauge pressure of the deethanizer 5 is 1.6-2.2MPa, the column top temperature is-30-39 ℃, preferably, the column top gauge pressure of the deethanizer 5 is 1.6-2MPa, and the column top temperature is-30-38 ℃, so as to separate components below C2 and components above C3 and C3.
Step 303: the components C2 and below C2 at the top of the column and the absorbent are fed to a demethanizer 6 to obtain a mixture of fuel gas at the top of the column and C2 components at the bottom of the column and the absorbent.
Specifically, in the setting of pressure and temperature, the top gauge pressure of the demethanizer 6 is 2.5-3.5MPa, the top temperature is-30-39 ℃, preferably, the top gauge pressure of the demethanizer 6 is 2.6-3.2MPa, and the top temperature is-30-38 ℃.
Ethylene was absorbed by the principle of gas-liquid equilibrium by adding propane absorbent at-30-38 deg.c to the top of the column.
Step 304: the mixture of the C2 component at the bottom and the absorbent is sent to the solvent recovery column 7 to obtain the C2 component at the top and the absorbent at the bottom, and the absorbent at the bottom is sent back to the demethanizer 6 again.
Specifically, in the setting of pressure and temperature, the top gauge pressure of the solvent recovery column 7 is 2.0-3.0MPa, the top temperature is-10-30 ℃, preferably, the top gauge pressure is 2.2-2.8MPa, the top temperature is-16-26 ℃, and the absorbent flow recovered at the bottom of the column is cooled to-30-38 ℃ and then is completely returned to the top of the demethanizer 6.
Step 305: the C2 component at the top of the tower is sent to an acetylene converter 8 for conversion and then sent to an ethylene rectifying tower 9 to obtain ethylene at the top of the tower and ethane at the bottom of the tower.
Specifically, the C2 component stream at the top of the tower is sent to an ethylene rectifying tower 9 for separating ethylene and ethane after being hydrotreated by an acetylene converter 8.
In the setting of pressure and temperature, the top gauge pressure of the ethylene rectifying tower 9 is 1.0-2.0MPa, the top temperature is-30-39 ℃, preferably, the top gauge pressure is 1.2-1.8MPa, and the top temperature is-30-38 ℃.
Structurally, the polymerization grade ethylene product is withdrawn through the side stream at the 2 nd to 10 th layer theoretical plates from the top of the column to the bottom of the column, and the bottom ethane stream is either taken as ethane product or sent to the fuel gas system; the ethylene rectifying tower 9 is provided with a middle boiling device at the position of 80-110 layers of theoretical plates from the top to the bottom, the material flow temperature at the position of the middle boiling device is-26-35 ℃, and the heat is supplied by adopting a refrigerant at-24 ℃; the reboiler at the bottom of the ethylene rectifying tower 9 adopts 7 ℃ refrigerant to supply heat.
Step 306: the C3 and C3 or more components at the bottom of the column are fed into the depropanizer 10 to obtain the C3 component at the top of the column and the C4 and C4 or more components at the bottom of the column.
Specifically, since the depropanizer 10 includes the high pressure depropanizer 1001 and the low pressure depropanizer 1002, in the setting of pressure and temperature, the top gauge pressure of the high pressure depropanizer 1001 is 1.8 to 2.3MPa, the top temperature is 40 to 80 ℃, preferably, the top pressure is 1.8 to 2.2MPa, the top temperature is 40 to 60 ℃; the low pressure depropanizer 1002 has a head pressure of 0.5 to 1.0MPa, a head temperature of 8 to 30 ℃, preferably 0.6 to 0.9MPa, and a head temperature of 10 to 20 ℃.
Wherein the bottom stream of the high pressure depropanizer 1001 exchanges heat with the top stream of the low pressure depropanizer 1002 by a heat exchanger 23, and the heat exchanged stream is sent to 2-12 layers of theoretical plates, preferably 3-10 layers of theoretical plates, from the top to the bottom of the low pressure depropanizer 1002.
Step 307: the C3 component at the top of the column is fed to a propylene rectifying column 11 to obtain propylene at the top of the column and propane at the bottom of the column.
Specifically, since the propylene rectification tower 11 comprises a first propylene rectification tower 1101 and a second propylene rectification tower 1102, the top gauge pressure of the second propylene rectification tower 1002 is 1.5-2.0MPa, the top temperature is 40-50 ℃, the top liquid phase of the tower extracts polymer grade propylene, and the bottom stream is sent to the first propylene rectification tower 1101. The top stream of the first propylene rectification tower 1101 is returned to the second propylene rectification tower 1102 and the bottom propane stream is sent out of the apparatus or make-up solvent recovery tower 7 for absorbent losses.
Step 308: the C4-stage C4 or higher components at the bottom of the column are fed to the debutanizer 12 to obtain the C4-stage C4 components at the top of the column and the C5 and higher components at the bottom of the column.
Specifically, in the setting of pressure and temperature, the gauge pressure at the top of the debutanizer 12 is 0.1-0.6MPa, the temperature at the top of the debutanizer is 40-50 ℃, the mixed C4 component of the liquid phase at the top of the debutanizer is sent out of the device or fed into a subsequent C4 cracking unit, and the components above C5 and C5 are mixed at the bottom of the device.
Proved by verification, the method can reduce the comprehensive energy consumption by 3-5% compared with the conventional common MTO olefin separation technology (mainly middle-cooling oil absorption mode demethanization) on the premise of not increasing equipment investment.
The ethylene product obtained by the invention accords with national standard GB/T7715-2014, the propylene product accords with national standard GB/T7716-2014, and the ethylene and propylene recovery rate can be more than 99.6%.
The separation method of the methanol-to-olefin gas of the embodiment of the invention comprises the steps of preprocessing a reaction product of the methanol-to-olefin reactor 20, and then sending the reaction product into a separator 2 for gas-liquid separation to obtain a gas-phase product and a condensate product; respectively sending the condensate product and the gas-phase product into a condensate dryer 3 and a first gas-phase dryer 4 for drying, and then sending the condensate product and the gas-phase product into a deethanizer 5 to obtain components below C2 and C2 at the top of the tower and components above C3 and C3 at the bottom of the tower; sending the components with the C2 and below C2 at the top of the tower and the absorbent into a demethanizer 6 to obtain a mixture of fuel gas at the top of the tower and the C2 component at the bottom of the tower and the absorbent; feeding the mixture of the C2 component and the absorbent at the bottom of the tower into a solvent recovery tower 7 to obtain the C2 component at the top of the tower and the absorbent at the bottom of the tower, and feeding the absorbent at the bottom of the tower back into the demethanizer 6 again; the C2 component at the top of the tower is sent to an acetylene converter 8 for conversion and then sent to an ethylene rectifying tower 9 to obtain ethylene at the top of the tower and ethane at the bottom of the tower; sending the C3 and above C3 components at the bottom of the tower into a depropanizer 10 to obtain the C3 components at the top of the tower and the C4 and above C4 components at the bottom of the tower; feeding the C3 component at the top of the tower into a propylene rectifying tower 11 to obtain propylene at the top of the tower and propane at the bottom of the tower; the components with more than C4 grade C4 at the bottom of the tower are sent into the debutanizer 12 to obtain the components with C4 grade at the top of the tower and the components with more than C5 grade C5 at the bottom of the tower, thereby realizing the separation of the gas for preparing olefin by methanol, changing the circulation loop of the absorbent used in the demethanizer 6 into the demethanizer 6-solvent recovery tower 7-demethanizer 6, shortening the circulation loop, not involving the deethanizer 5 and the propylene rectifying tower 11, effectively reducing the load, energy consumption and equipment investment of the deethanizer 5 and the propylene rectifying tower 11, and improving the stability of the device.
The foregoing description is only for the convenience of those skilled in the art to understand the technical solution of the present invention, and is not intended to limit the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A methanol-to-olefin gas separation apparatus, comprising: pretreatment module (1), separator (2), condensate dryer (3), first gas phase dryer (4), deethanizer (5), demethanizer (6), solvent recovery column (7), acetylene converter (8), ethylene rectifying column (9), depropanizer (10), propylene rectifying column (11), debutanizer (12), water collector (22), heat exchanger (23) and second gas phase dryer (25), wherein:
the preprocessing assembly (1) comprises: a quench tower (101), a water stripper (102), a methanol recovery tower (103), a first compressor section (104), a second compressor section (105), a water scrubber (106), a third compressor section (107) and a caustic scrubber (108), wherein the top outlet of the quench tower (101) is communicated with the inlet of the methanol recovery tower (103), the top outlet of the methanol recovery tower (103) is communicated with the inlet of the first compressor section (104), the outlet of the first compressor section (104) is communicated with the inlet of the second compressor section (105), the outlet of the second compressor section (105) is communicated with the inlet of the water scrubber (106), the outlet of the water scrubber (106) is communicated with the inlet of the third compressor section (107), the outlet of the third compressor section (107) is communicated with the inlet of the caustic scrubber (108), the bottom outlet of the quench tower (101) is communicated with the inlet of the first compressor section (104), the outlet of the methanol recovery tower (103) is communicated with the inlet of the caustic scrubber (102), the outlet of the bottom (103) is communicated with the outlet of the caustic scrubber (102), and the outlet of the water stripper (2);
the gas phase outlet of the separator (2) is communicated with the inlet of the first gas phase dryer (4), the condensate outlet of the separator (2) is communicated with the inlet of the condensate dryer (3), the condensate dryer (3) is communicated with the liquid phase inlet of the deethanizer (5), the outlet of the first gas phase dryer (4) is communicated with the gas phase inlet of the deethanizer (5), the top outlet of the deethanizer (5) is communicated with the tower body inlet of the demethanizer (6), and the top outlet of the demethanizer (6) is communicated with the fuel gas collector (13);
the bottom outlet of the demethanizer (6) is communicated with the inlet of the solvent recovery tower (7), the bottom outlet of the solvent recovery tower (7) is communicated with the top inlet of the demethanizer (6), the top outlet of the solvent recovery tower (7) is communicated with the inlet of the acetylene converter (8), and the outlet of the acetylene converter (8) is communicated with the inlet of the ethylene rectification tower (9) through the second gas phase dryer (25);
the ethylene rectifying tower (9) is internally provided with a middle boiler, a reboiler and a side line, wherein the middle boiler is arranged at 80-110 layers of theoretical plates from the top of the ethylene rectifying tower (9) to the bottom of the ethylene rectifying tower, the reboiler is arranged at the bottom of the ethylene rectifying tower (9), the side line is arranged at 2-10 layers of theoretical plates from the top of the ethylene rectifying tower (9) to the bottom of the ethylene rectifying tower, the side line is communicated with the ethylene collector (14), and the bottom outlet of the ethylene rectifying tower (9) is communicated with the ethane collector (15);
the depropanizer (10) comprises a high-pressure depropanizer (1001) and a low-pressure depropanizer (1002), wherein a bottom outlet of the deethanizer (5) is communicated with an inlet of the high-pressure depropanizer (1001), a bottom outlet of the high-pressure depropanizer (1001) is communicated with 3-10 layers of theoretical baffles from the top of the tower to the bottom of the low-pressure depropanizer (1002) through the heat exchanger (23), and a top outlet of the low-pressure depropanizer (1002) is communicated with an inlet of the high-pressure depropanizer (1001) through the heat exchanger (23);
the propylene rectification tower (11) comprises a first propylene rectification tower (1101) and a second propylene rectification tower (1102), wherein the top outlet of the high-pressure depropanization tower (1001) is communicated with the inlet of the first propylene rectification tower (1101), the top outlet of the first propylene rectification tower (1101) is communicated with a propylene collector (16), the bottom outlet of the first propylene rectification tower (1101) is communicated with the inlet of the second propylene rectification tower (1102), the top outlet of the second propylene rectification tower (1102) is communicated with the inlet of the first propylene rectification tower (1101), and the bottom outlet of the second propylene rectification tower (1102) is communicated with a propane collector (17) and the solvent recovery tower (7);
the bottom outlet of the low-pressure depropanizer (1002) is communicated with the inlet of the debutanizer (12), the top outlet of the debutanizer (12) is communicated with a C4 component collector (18), and the bottom outlet of the debutanizer (12) is communicated with a C5 and above C5 component collector (19).
2. The separation device of methanol-to-olefin gas according to claim 1, characterized in that the pretreatment assembly (1) further comprises a spent lye pretreatment column (109);
the inlet of the quenching tower (101) is communicated with the methanol-to-olefin reactor (20);
the bottom outlet of the alkali washing tower (108) is communicated with the inlet of the waste lye pretreatment tower (109), and the outlet of the waste lye pretreatment tower (109) is communicated with the waste lye collector (21).
3. The methanol-to-olefin gas separation apparatus according to claim 1, characterized by further comprising: a compressor four-stage (24);
the compressor four stage (24) is disposed between the deethanizer (5) and the demethanizer (6).
4. A method for separating a methanol-to-olefin gas, the method comprising:
pretreating a reaction product of a methanol-to-olefin reactor (20), wherein the pretreatment comprises the steps of feeding the reaction product into a quenching tower (101) to obtain a cooled gas phase component at the top of the tower and a cooled liquid phase component at the bottom of the tower, feeding the cooled gas phase component at the top of the tower into a methanol recovery tower (103) to obtain a recovered gas phase component at the top of the tower and a recovered liquid phase component at the bottom of the tower, feeding the cooled liquid phase at the bottom of the tower and the recovered liquid phase component at the bottom of the tower into a water stripping tower (102) to obtain purified water, feeding the purified water into a water collector (22) to collect, and feeding the recovered gas phase component at the top of the tower into a first compressor section (104), a second compressor section (105), a water washing tower (106), a third compressor section (107) and a caustic washing tower (108) in sequence to obtain a pretreated reaction product;
sending the pretreated reaction product into a separator (2) for gas-liquid separation to obtain a gas-phase product and a condensate product;
the gas phase product and the condensate product are respectively sent into a first gas coherent dryer (4) and a condensate dryer (3) for drying and then sent into a deethanizer (5) to obtain components below C2 and C2 at the top of the tower and components above C3 and C3 at the bottom of the tower;
sending the components with the C2 and below C2 at the top of the tower and the absorbent into a demethanizer (6) to obtain a mixture of fuel gas at the top of the tower, the C2 component at the bottom of the tower and the absorbent;
feeding the mixture of the C2 component and the absorbent at the bottom of the tower to a solvent recovery tower (7) to obtain the C2 component at the top of the tower and the absorbent at the bottom of the tower, and feeding the absorbent at the bottom of the tower back to the demethanizer (6) again;
sending the C2 component at the top of the tower into an acetylene converter (8) for conversion, and then sending the C2 component to an ethylene rectifying tower (9) through a second gas phase dryer (25) to obtain ethylene at the top of the tower and ethane at the bottom of the tower, wherein an intermediate boiler is arranged at an 80 th-110 th layer theoretical plate from the top of the ethylene rectifying tower (9) to the bottom of the tower, a reboiler is arranged at the bottom of the ethylene rectifying tower (9), a side line is arranged at the 2 nd-10 th layer theoretical plate from the top of the ethylene rectifying tower (9) to the bottom of the tower, the side line is communicated with an ethylene collector (14), and the second gas phase dryer (25) is used for removing product water generated after the C2 component at the top of the tower is converted by the acetylene converter (8);
sending the components with the carbon number of 3 and more than 3 at the bottom of the tower to a high-pressure depropanizer (1001) to obtain the components with the carbon number of 3 at the top of the high-pressure depropanizer and the components with the carbon number of 4 and more than 4 at the bottom of the high-pressure depropanizer, sending the components with the carbon number of 4 and more than 4 at the bottom of the high-pressure depropanizer to a low-pressure depropanizer (1002) through a heat exchanger (23), and sending the components with the carbon number of 4 and more than 4 at the bottom of the low-pressure depropanizer to the high-pressure depropanizer (1001), wherein the components with the carbon number of 4 and more than 4 at the bottom of the high-pressure depropanizer and the components with the carbon number of 3 at the top of the low-pressure depropanizer are mutually exchanged at the heat exchanger (23);
feeding the C3 component at the top of the high-pressure depropanizer into a first propylene rectifying tower (1101) to obtain propylene at the top of the first propylene rectifying tower and propane at the bottom of the first propylene rectifying tower, feeding the propane at the bottom of the first propylene rectifying tower into a second propylene rectifying tower (1102) to obtain propylene at the top of the second propylene rectifying tower and propane at the bottom of the second propylene rectifying tower, feeding the propylene at the top of the second propylene rectifying tower into the first propylene rectifying tower (1101) for rectifying again, and feeding the propane at the bottom of the second propylene rectifying tower into a propane collector (17) and a solvent recovery tower (7) to supplement the loss of the absorbent;
and C4 and above C4 components at the bottom of the low-pressure depropanizer are sent into a debutanizer (12) to obtain C4 components at the top of the tower and C5 and above C5 components at the bottom of the tower.
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