CN111960920B - Material recovery equipment and material recovery method for DAVY methanol synthesis device - Google Patents
Material recovery equipment and material recovery method for DAVY methanol synthesis device Download PDFInfo
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- CN111960920B CN111960920B CN202010827912.1A CN202010827912A CN111960920B CN 111960920 B CN111960920 B CN 111960920B CN 202010827912 A CN202010827912 A CN 202010827912A CN 111960920 B CN111960920 B CN 111960920B
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- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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Abstract
The invention relates to the field of methanol preparation, and discloses material recovery equipment and a material recovery method for a DAVY methanol synthesis device. The apparatus comprises: the first gas-liquid separation unit is used for carrying out gas-liquid separation on the process gas from the crude methanol water cooler to obtain a first liquid phase and a first non-condensable gas; a flash unit for flashing the first liquid phase from the gas-liquid separation unit; a cooling unit for cooling the gas from the flash unit; and the second gas-liquid separation unit is used for receiving the product cooled by the cooling unit, performing gas-liquid separation, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation. The invention can provide the material recovery equipment and the material recovery method for the DAVY methanol synthesis device, which have the advantages of low cost, simple process and high material recovery efficiency.
Description
Technical Field
The invention relates to the field of methanol preparation, in particular to material recovery equipment and a material recovery method for a DAVY methanol synthesis device.
Background
In recent years, with the rapid development of coal chemical industry, more and more large methanol synthesis devices are built and put into production, the methanol synthesis technology is mature at present and presents a prosperous development situation, the methanol synthesis technology mainly comprises a high-pressure method, a medium-pressure method and a low-pressure method, and the low-pressure method has more advantages and has obvious advantages in the aspects of energy consumption, equipment investment, single tower yield, profit and the like. The DAVY methanol synthesis system mainly comprises two series-parallel coupled steam rising type synthesis towers, wherein the synthesis towers are radial flow towers, gas generates a methanol synthesis reaction through a catalyst filled on the shell side, the temperature of a catalyst bed layer is adjusted through the inlet temperature of the synthesis towers and the pressure of a steam drum, and byproduct steam is sent out of a boundary area after being overheated.
The current technological process of the DAVY methanol synthesis device is as follows: crude methanol from No. 1 and No. 2 crude methanol separators enters a crude methanol flash tank, after pressure reduction, flash gas is sent to a steam superheater to be used as fuel gas, the crude methanol after flash evaporation is sent to a stabilizing tower, tower gas is sent to a stabilizing tower pre-condenser to condense most of methanol in the tower gas, methanol liquid under condensation enters a stabilizing tower reflux tank, gas phase under non-condensation is condensed by a stabilizing tower condenser, the methanol liquid under condensation enters a stabilizing tower reflux tank, noncondensable gas containing low-boiling-point substances and a small amount of methanol which is still not condensed is sent to a PSA system after pressure reduction, and the noncondensable gas is sent to the steam superheater to be used as fuel after being boosted by a tail gas compressor. The methanol liquid in the reflux tank of the stabilizing tower is pressurized by a reflux pump and then sent back to the stabilizing tower to be used as reflux liquid.
The tower bottom of the stabilizer is provided with a reboiler, the heat source is low-pressure saturated steam of 0.46MPa, and the methanol at the tower bottom of the stabilizer is pressurized by an MTO-grade methanol pump, then sent to an MTO-grade methanol cooler, and then sent to an MTO-grade methanol finished product tank area after being cooled. Due to the design and the working condition, a large amount of flash steam, particularly the tail stage of the catalyst, is directly sent to the steam superheater to be used as fuel gas, and the flash steam contains a large amount of crude methanol which is not well recycled, so that the white water is lost to be used as the fuel gas, the benefit is not better enlarged, and the energy consumption of the device is increased.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provide a material recovery device and a material recovery method for a DAVY methanol synthesis device, which have the advantages of low cost, simple process and high material recovery efficiency.
In order to achieve the above object, an aspect of the present invention provides a material recycling apparatus for a DAVY methanol synthesis plant, the apparatus comprising:
the first gas-liquid separation unit is used for carrying out gas-liquid separation on the process gas from the crude methanol water cooler to obtain a first liquid phase and a first non-condensable gas;
a flash unit for flashing the first liquid phase from the gas-liquid separation unit;
a cooling unit for cooling the gas from the flash unit; and
and the second gas-liquid separation unit is used for receiving the product cooled by the cooling unit, performing gas-liquid separation, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation.
Preferably, the first gas-liquid separation unit is a vane-type gas-liquid separator.
Preferably, the first gas-liquid separation unit further has a pipe for discharging the first non-condensable gas separated by the gas-liquid separation unit, and the pipe is connected to the compression unit.
Preferably, the flash unit is one of a flash drum, a flash drum and a flash column.
Preferably, the cooling unit is connected to the top of the flash unit.
Preferably, one end of the second gas-liquid separation unit is connected with the cooling unit, and the other end of the second gas-liquid separation unit is connected with the flash evaporation unit.
Preferably, the cooling unit is an air cooler or a water cooler.
Preferably, the second gas-liquid separation unit is a wire-mesh type gas-liquid separator or a packing type gas-liquid separator.
The present invention also provides a method for material recovery carried out in a material recovery apparatus for a DAVY methanol synthesis plant according to the present invention, wherein the method comprises the steps of,
1) Carrying out first gas-liquid separation on the process gas from the crude methanol water cooler in the first gas-liquid separation unit to obtain a first liquid phase and a first non-condensable gas;
2) Flashing the first liquid phase from the gas-liquid separation unit in the flash unit;
3) Cooling the gas from the flash unit in the cooling unit;
4) And performing second gas-liquid separation on the product cooled by the cooling unit in a second gas-liquid separation unit, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation.
Preferably, the method further comprises feeding the first gas phase separated by the first gas-liquid separation unit to the compression unit for compression.
According to the method provided by the invention, the material recovery equipment and the material recovery method for the DAVY methanol synthesis device have the advantages of low cost, simple process and high material recovery efficiency.
In addition, the invention realizes multiple purposes of saving cost, reducing consumption, protecting environment, maximally utilizing energy and maximizing benefit by using a large amount of entrained methanol in the original fuel gas and the effective gas in the original torch gas through the condensing equipment, the separating equipment and the pressure raising equipment.
Drawings
FIG. 1 is a schematic of a feed recovery apparatus for a DAVY methanol synthesis plant of the present invention.
Description of the reference numerals
V201: a first gas-liquid separation unit; v301: a flash unit; v3011: a cooling unit: v3012: a second gas-liquid separation unit; v401: and a compression unit.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
FIG. 1 is a schematic of a feed recovery apparatus for a DAVY methanol synthesis plant of the present invention. As shown in fig. 1, the material recovery apparatus for a DAVY methanol synthesis plant provided by the present invention comprises:
the first gas-liquid separation unit V201 is used for carrying out gas-liquid separation on the process gas from the crude methanol water cooler to obtain a first liquid phase and a first non-condensable gas;
a flash unit V301 for flashing the first liquid phase from the gas-liquid separation unit;
a cooling unit V3011 for cooling the gas from the flash unit; and
and the second gas-liquid separation unit V3012 is used for receiving the product cooled by the cooling unit, performing gas-liquid separation, returning a second liquid phase obtained through gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained through gas-liquid separation.
In the invention, the process gas from the crude methanol water cooler refers to the process gas after the reaction gas at the outlet of the methanol synthesis tower passes through the crude methanol air cooler and the crude methanol water cooler, and the main components of the process gas comprise crude methanol generated after the reaction, unreacted hydrogen, carbon monoxide, carbon dioxide, part of inert gases such as methane, nitrogen, argon and the like.
According to the present invention, the first gas-liquid separation unit V201 may be various apparatuses commonly used in the art for gas-liquid separation, for example, may be one or more of a vane-type gas-liquid separator, a packing-type gas-liquid separator, and a gravity settling-type gas-liquid separator; preferably, the first gas-liquid separation unit V201 is a vaned gas-liquid separator. The number of the first gas-liquid separation units V201 may be 1, or may be plural, and for example, may be 1, 2, or 3, and preferably 2.
According to the present invention, preferably, the first gas-liquid separation unit V201 further has a pipeline for discharging the first non-condensable gas separated by the gas-liquid separation unit V201, the pipeline is connected to the compression unit V401 (preferably, connected to the top of the compression unit V401), and the compression unit V401 is configured to re-pressurize the gas phase separated by the first gas-liquid separation unit V201 by the compression unit and return the gas phase to the methanol synthesis tower to react again to produce crude methanol under the action of the catalyst.
The compression unit V401 may be a compressor, for example.
According to the present invention, the flash unit V301 may be various equipments commonly used in the art for flash evaporation, preferably, the flash unit V301 is one of a flash drum, a flash drum and a flash column; more preferably, the flash unit V301 is a flash drum.
According to the present invention, the cooling unit V3011 may be various devices used for cooling in the art, and preferably, the cooling unit V3011 is an air cooler or a water cooler.
According to the invention, the cooling unit V3011 is connected to the top of the flash unit V301.
According to the present invention, the second gas-liquid separation unit V3012 may be various devices generally used for gas-liquid separation in the art, and is preferably a wire type gas-liquid separator or a packing type gas-liquid separator.
According to the present invention, it is preferable that one end of the second gas-liquid separation unit V3012 is connected to the cooling unit V3011, and the other end is connected to the flash evaporation unit V301.
According to the present invention, preferably the bottom of the flash unit V301 is connected via a pipe to a stabilizer column in the DAVY methanol synthesis plant.
The present invention also provides a method for material recovery carried out in a material recovery apparatus for a DAVY methanol synthesis plant according to the present invention, wherein the method comprises the steps of,
1) Performing first gas-liquid separation on the process gas from the crude methanol water cooler in the first gas-liquid separation unit V201 to obtain a first liquid phase and a first non-condensable gas;
2) Flashing the first liquid phase from the first gas-liquid separation unit in the flash unit V301;
3) Cooling the gas from the flash unit in the cooling unit V3011;
4) And performing second gas-liquid separation on the product cooled by the cooling unit in a second gas-liquid separation unit V3012, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation.
Preferably, the method further comprises sending the first gas phase separated by the first gas-liquid separation unit V201 to the compression unit V401 for compression. The first gas phase separated by the first gas-liquid separation unit V201 is subjected to secondary pressure increase by the compression unit and then returns to the methanol synthesis tower to react again under the action of the catalyst to produce the crude methanol.
According to the invention, the methanol content in the process gas from the crude methanol water cooler in step 1) can be, for example, from 1 to 4mol%, preferably from 2 to 4mol%.
Preferably, the temperature of the first gas-liquid separation is below 45 ℃, preferably 30-45 ℃. The gas-liquid separation can be sufficiently performed at the above temperature.
According to the present invention, in step 2), before the first liquid phase from the first gas-liquid separation unit is flashed in the flash unit V301, the first liquid phase is preferably subjected to solid-liquid separation to remove impurities such as paraffin, which is a side reaction product. The method of solid-liquid separation is not particularly limited, and may be, for example, filtration, centrifugation or the like.
According to the present invention, preferably, in step 2), the temperature of the flash may be, for example, 40 to 50 ℃, for example, 45 ℃.
According to the present invention, preferably, in step 3), the gas from the flash unit is cooled with air, water or the like.
According to the invention, the temperature of the cooling in step 3) is preferably 33 to 37 ℃, for example 35 ℃.
According to the present invention, preferably, in the step 4), the second gas-liquid separation separates a gas-phase non-condensable gas and a liquid-phase in a wire-type gas-liquid separator.
According to the present invention, preferably, in the step 4), the temperature of the second gas-liquid is 33 to 37 ℃, for example, may be 35 ℃.
According to the present invention, in step 4), the content of methanol in the second non-condensable gas is preferably 2mol% or less, and more preferably 1mol% or less.
In a preferred embodiment of the present invention, the process gas from the crude methanol water cooler enters the first gas-liquid separation unit V201 for gas-liquid separation, the first liquid phase (crude methanol) separated by the first gas-liquid separation unit V201 is sent to the flash evaporation unit V301 for flash evaporation, the gas phase at the top of the flash evaporation unit V301 is cooled by the cooling unit V3011 and then enters the second gas-liquid separation unit V3012 for gas-liquid separation, the second liquid phase obtained by gas-liquid separation is returned to the flash evaporation unit V301 again for flash evaporation, and the rest of the second non-condensable gas is sent to the steam superheater for combustion; in addition, the first non-condensable gas separated by the first gas-liquid separation unit V201 is sent to the compression unit V401 (circulating gas compressor) for compression, and the compressed gas returns to the methanol synthesis loop methanol synthesis tower for reaction.
The present invention will be described below with reference to examples, but the present invention is not limited to the following examples.
Example 1
As shown in fig. 1, the process gas (methanol content is about 3 mol%) from the crude methanol water cooler is filtered to remove impurities such as paraffin, and then enters a first gas-liquid separation unit V201 (specifically, a vane-type gas-liquid separator) for gas-liquid separation (gas-liquid separation temperature is 45 ℃), the first liquid phase (crude methanol) separated by the first gas-liquid separation unit V201 is sent to a flash unit V301 (specifically, a flash tower) for flash evaporation (flash evaporation temperature is 45 ℃), the gas phase at the top of the flash unit V301 is cooled to 35 ℃ by a cooling unit V3011 (specifically, an air cooler), and then enters a second gas-liquid separation unit V3012 (specifically, a screen-type gas-liquid separator) for gas-liquid separation (gas-liquid separation temperature is 35 ℃), the second liquid phase obtained by gas-liquid separation is returned to the flash unit V301 for flash evaporation again, and the rest of second non-condensable gas (methanol content is less than 1 mol%) is sent to a steam superheater for combustion; in addition, the first non-condensable gas separated by the first gas-liquid separation unit V201 is sent to the compression unit V401 (recycle gas compressor) for compression, and the compressed gas returns to the methanol synthesis loop methanol synthesis tower again for reaction.
By the method, a large amount of entrained methanol in the original fuel gas and the effective gas in the original torch gas can pass through the condensing equipment, the separating equipment and the pressure raising equipment to achieve multiple purposes of saving cost, reducing consumption, protecting environment, maximally utilizing energy and maximizing benefit.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (8)
1. A material withdrawal apparatus for a DAVY methanol synthesis plant, the apparatus comprising:
the first gas-liquid separation unit is used for carrying out gas-liquid separation on the process gas from the crude methanol water cooler to obtain a first liquid phase and a first non-condensable gas;
a flash unit for flashing the first liquid phase from the gas-liquid separation unit;
a cooling unit for cooling the gas from the flash unit; and
a second gas-liquid separation unit for receiving the product cooled by the cooling unit, performing gas-liquid separation, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation,
wherein the first gas-liquid separation unit is a vane type gas-liquid separator,
the first gas-liquid separation unit is also provided with a pipeline for discharging the first non-condensable gas separated by the gas-liquid separation unit, and the pipeline is connected with the compression unit.
2. The material recovery apparatus of claim 1, wherein the flash unit is one of a flash tank, a flash drum, and a flash column.
3. The material recovery apparatus of claim 2, wherein the cooling unit is connected to a top of the flash unit.
4. The material recovery apparatus according to claim 2, wherein the second gas-liquid separation unit is connected to the cooling unit at one end and to the flash unit at the other end.
5. The material reclaiming apparatus according to any one of claims 1 to 4, wherein the cooling unit is an air cooler or a water cooler.
6. The material recovery apparatus according to any one of claims 1 to 4, wherein the second gas-liquid separation unit is a wire-type gas-liquid separator or a packed gas-liquid separator.
7. A method for material recovery, characterized in that it is carried out in a material recovery plant for a DAVY methanol synthesis plant according to any one of claims 1 to 6, wherein it comprises the following steps,
1) Carrying out first gas-liquid separation on the process gas from the crude methanol water cooler in the first gas-liquid separation unit to obtain a first liquid phase and a first non-condensable gas;
2) Flashing the first liquid phase from the gas-liquid separation unit in the flash unit;
3) Cooling the gas from the flash unit in the cooling unit;
4) And performing second gas-liquid separation on the product cooled by the cooling unit in a second gas-liquid separation unit, returning a second liquid phase obtained by gas-liquid separation to the flash evaporation unit for flash evaporation, and discharging a second non-condensable gas obtained by gas-liquid separation.
8. The process according to claim 7, further comprising feeding the first gas phase separated in the first gas-liquid separation unit to the compression unit for compression.
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| CN202010827912.1A CN111960920B (en) | 2020-08-17 | 2020-08-17 | Material recovery equipment and material recovery method for DAVY methanol synthesis device |
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| CN202010827912.1A CN111960920B (en) | 2020-08-17 | 2020-08-17 | Material recovery equipment and material recovery method for DAVY methanol synthesis device |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107823906A (en) * | 2017-09-19 | 2018-03-23 | 鲁西化工集团股份有限公司 | A kind of raw gas conversion process condensate liquid stripping processing system and method |
| WO2018115596A1 (en) * | 2016-12-23 | 2018-06-28 | Avefori Oy | Method and system for manufacturing methanol from organic waste |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018115596A1 (en) * | 2016-12-23 | 2018-06-28 | Avefori Oy | Method and system for manufacturing methanol from organic waste |
| CN107823906A (en) * | 2017-09-19 | 2018-03-23 | 鲁西化工集团股份有限公司 | A kind of raw gas conversion process condensate liquid stripping processing system and method |
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