CN114733223A - Method for recovering condensate - Google Patents
Method for recovering condensate Download PDFInfo
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- CN114733223A CN114733223A CN202210323410.4A CN202210323410A CN114733223A CN 114733223 A CN114733223 A CN 114733223A CN 202210323410 A CN202210323410 A CN 202210323410A CN 114733223 A CN114733223 A CN 114733223A
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- steam
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
- B01D5/0006—Coils or serpentines
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention relates to a condensate recovery mode, and belongs to the technical field of methanol production. According to the invention, a recovery device is adopted to recycle steam in the production process, a cooling tower and an auxiliary heat exchanger are arranged among a refining tank, a dry quenching tank and a loading and unloading station, backflow steam and heat tracing steam cooled by an original main heat exchanger are subjected to heat exchange firstly, the temperature of the backflow steam is lower, the backflow steam is contacted with the heat tracing steam cooled by full heat exchange firstly, the backflow steam is gradually heated in an outer pipe, and the heat tracing steam is gradually cooled in the inner pipe, so that the temperature difference between the heat tracing steam and the backflow steam during heat exchange is not large, the problem of severe vibration generated when the high-temperature heat tracing steam and the low-temperature backflow steam are mixed in the prior art is effectively solved, and the production risk is reduced; meanwhile, the heat exchange conditions of the heat tracing steam and the reflux steam are controlled by a temperature sensor and a pneumatic ball valve, the temperature of the primary cold steam after heat exchange and mixing is controlled to be 70-80 ℃, and the steam is fully condensed in the secondary heat exchanger.
Description
Technical Field
The invention belongs to the technical field of methanol production, and particularly relates to a condensate recovery mode.
Background
The coal and coke are the main solid fuel for producing raw material gas of methanol, and the technological route for producing methanol by using coal and coke includes gasification of fuel, desulfurization of gas, conversion, decarbonization and synthesis and refining of methanol. In the production process, a large amount of high-temperature heat tracing steam can be generated in a coking refined benzene tank area and a loading and unloading station, the temperature of the steam can reach 140 ℃, the heat tracing steam can be generally sent into a dry quenching workshop through a pipeline which is merged into a pipeline of a main heat exchanger for the purpose of fully utilizing resources, the temperature of the steam cooled by a main cooler is about 40 ℃, and when the high-temperature heat tracing steam converges, severe vibration is generated due to large temperature difference, so that the high-temperature heat tracing steam is a great hidden danger for safety production.
Disclosure of Invention
In order to solve the technical problems mentioned in the background art, the invention provides a condensate recovery mode.
The purpose of the invention can be realized by the following technical scheme:
a method for condensate recovery, comprising the steps of:
step S1: introducing the heat tracing steam of the refining tank and the loading and unloading station into a buffer tank of a recovery device for collection and pressurization;
step S2: introducing the pressurized heat tracing steam into an inner pipe of a cooling tower, carrying out heat exchange step by step on the heat tracing steam and reflux steam in the cooling tower, and mixing after heat exchange to obtain primary cooling steam;
step S3: introducing the primary cooling steam into an auxiliary heat exchanger for heat exchange and temperature reduction and gas-liquid separation to respectively obtain auxiliary condensate and final cooling steam, recycling the auxiliary condensate, introducing the final cooling steam into an annular flue gas channel of the dry quenching tank, and cooling red coke in the dry quenching tank;
step S4: and final-cooling steam is subjected to heat exchange and temperature rise in the dry quenching tank and then is introduced into the main heat exchanger for cooling and gas-liquid separation to respectively obtain main condensate and reflux steam, the main condensate is recycled, the reflux steam is introduced into the outer pipe of the cooling tower, and the reflux steam and the heat tracing steam in the inner pipe carry out heat convection so as to realize circulating condensation of the heat tracing steam.
Preferably, the heat tracing steam in the buffer tank is pressurized to 8-12bar, which can meet the transportation of the heat tracing steam.
Preferably, the temperature of the primary cooling steam is 70-80 ℃, the primary cooling steam is obtained by mixing heat tracing steam and return steam after heat exchange, and the primary cooling steam can be cooled and used in the dry quenching process after being subjected to primary cooling and heat exchange with air through a fin type heat exchanger.
Preferably, the temperature of the final cooling steam is 40-50 ℃, and the temperature is set to facilitate the rapid heat exchange of the red coke.
Preferably, the temperature of the reflux steam is 32-45 ℃, the heat exchange efficiency of the main heat exchanger is high under the temperature setting, and the heat exchange efficiency of the reflux steam and the heat tracing steam is high, so that the heat tracing steam is more economical.
Furthermore, the recovery device comprises a refining tank, a dry quenching tank and a loading and unloading station, wherein the heat tracing steam outlet ends of the refining tank and the loading and unloading station are both communicated with a buffer tank, and the buffer tank is at least internally provided with a gas storage tank and a booster pump and is used for boosting heat tracing steam and collecting the boosted heat tracing steam;
the steam outlet end of the buffer tank is communicated with a cooling tower, the cooling tower comprises an outer pipe and an inner pipe fixed in the outer pipe, a partition plate is hermetically connected between the outer pipe and the inner pipe, an interlayer between the outer pipe and the inner pipe is partitioned into a plurality of heat exchange intervals, the flow of reflux steam in each heat exchange interval is convenient to control, so that the heat exchange condition is controlled, a spiral partition plate is arranged in each heat exchange interval, the reflux steam and the heat tracing steam can fully exchange heat, the outer pipe is also communicated with a flow control pipeline, the adjacent heat exchange intervals are communicated through the flow control pipeline, and a temperature sensor and a pneumatic ball valve are arranged on the flow control pipeline and used for detecting the temperature of the reflux steam and controlling the flow of the reflux steam;
the steam inlet end of the inner pipe is far away from the steam inlet end of the outer pipe, so that the heat tracing steam and the backflow steam generate convection, the heat exchange efficiency is increased, the steam outlet end of the inner pipe is communicated with the steam outlet end of the outer pipe, the heat tracing steam after heat exchange is mixed with the backflow steam, the steam outlet ends of the inner pipe and the outer pipe are communicated and then communicated with the auxiliary heat exchanger, the auxiliary heat exchanger is a fin heat exchanger, the mixed steam is subjected to heat exchange, a gas-liquid separator is arranged in the auxiliary heat exchanger, condensate is separated from the steam, the steam outlet end of the auxiliary heat exchanger is communicated with the annular flue gas channel of the dry quenching tank, the steam outlet end of the dry quenching tank is communicated with a main heat exchanger, the main heat exchanger is a water-cooled heat exchanger and is used for forcibly exchanging heat for the steam after heat exchange of the dry quenching tank, the main heat exchanger is provided with the gas-liquid separator, and the steam outlet end of the main heat exchanger is communicated with the steam inlet end of the outer pipe.
The invention has the beneficial effects that:
1. according to the invention, the cooling tower and the auxiliary heat exchanger are arranged among the refining tank, the dry quenching tank and the loading and unloading station, the return steam and the heat tracing steam cooled by the original main heat exchanger are subjected to heat exchange firstly, the temperature of the return steam is lower, the return steam is contacted with the heat tracing steam firstly after sufficient heat exchange and cooling, the temperature of the return steam is gradually increased in the outer pipe, and the temperature of the heat tracing steam is gradually reduced in the inner pipe, so that the temperature difference between the heat tracing steam and the return steam is not large during heat exchange, the problem of severe vibration generated when the high-temperature heat tracing steam and the low-temperature return steam are mixed in the prior art is effectively solved, and the production risk is reduced.
2. The invention can control the heat exchange conditions of the heat tracing steam and the reflux steam through the temperature sensor and the pneumatic ball valve, control the temperature of the primary cooling steam after heat exchange and mixing to be 70-80 ℃, approach the temperature of the condensate at the temperature and be beneficial to fully condensing the steam in the auxiliary heat exchanger.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the description below are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of the recycling apparatus of the present invention;
FIG. 2 is a schematic external view of a cooling tower according to the present invention;
FIG. 3 is a schematic view of the internal structure of the cooling tower of the present invention.
In the figure:
11. a refining tank; 12. a cooling tower; 13. a primary heat exchanger; 14. a dry quenching tank; 15. a loading and unloading station; 16. a secondary heat exchanger; 17. a buffer tank; 21. a flow control pipeline; 22. a temperature sensor; 23. a pneumatic ball valve; 31. an inner tube; 32. an outer tube; 33. partition plates; 34. a spiral separator.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Referring to fig. 1-3, the embodiment provides a recycling device, which includes a refining tank 11, a dry quenching tank 14 and a loading and unloading station 15, wherein the heat tracing steam of the refining tank 11 and the loading and unloading station 15 is communicated with a buffer tank 17 through a pipeline, the buffer tank 17 is equipped with a gas storage tank and a booster pump, the collected heat tracing steam is pressurized, collected and stored, a driving force is provided for the circulation of the heat tracing steam, the pressurization pressure is 8-12bar, the transportation of the heat tracing steam can be satisfied under the pressure, the gas flow can be controlled conveniently, and the adjustment is performed according to the actual recycling device specification;
the steam outlet end of the buffer tank 17 is communicated with a cooling tower 12, the cooling tower 12 comprises an outer pipe 32 and an inner pipe 31 fixed in the outer pipe 32, both ends of the inner pipe 31 are provided with connecting flanges for communicating heat tracing steam, a partition plate 33 is hermetically connected between the outer pipe 32 and the inner pipe 31, an interlayer between the outer pipe 32 and the inner pipe 31 is divided into four heat exchange sections, the flow of the reflux steam in each heat exchange section is convenient to control, thereby controlling the heat exchange condition, a spiral partition plate 34 is arranged in each heat exchange section, so that the reflux steam and the heat tracing steam can fully exchange heat, the outer pipe 32 is also communicated with a flow control pipeline 21, the adjacent heat exchange sections are communicated through the flow control pipeline 21, the flow control pipeline 21 is provided with a temperature sensor 22 and a pneumatic ball valve 23 for detecting the temperature of the reflux steam and controlling the flow of the reflux steam, the upper end and the lower end of the outer pipe 32 are communicated with the connecting flanges, be used for letting in backward flow steam, and set up the steam inlet end flange one side of keeping away from outer tube 32 with the steam inlet end flange of inner tube 31, the temperature of backward flow steam is lower, with abundant heat transfer cooling back companion's heat steam contact earlier, backward flow steam heaies up gradually in outer tube 32, companion's heat steam cools down gradually in inner tube 31, make companion's heat steam and backward flow steam the difference in temperature when the heat transfer not big, effectively solve the vibration problem that produces when high temperature companion's heat steam mixes with low temperature backward flow steam among the prior art, avoid the safety risk through cooling tower 12.
The steam outlet end connecting flange of the inner pipe 31 is communicated with the steam outlet end connecting flange of the outer pipe 32 through a pipeline, one end of the pipeline is communicated with the auxiliary heat exchanger 16, the auxiliary heat exchanger 16 is used for further cooling the steam mixed with heat exchange, usually, a fin type heat exchanger is selected for heat exchange with air, a gas-liquid separator is configured in the auxiliary heat exchanger 16 to separate condensate from the steam, the steam outlet end of the auxiliary heat exchanger 16 is communicated with an annular flue gas channel of the dry quenching tank 14, the steam outlet end of the dry quenching tank 14 is communicated with the main heat exchanger 13, the main heat exchanger 13 is a water-cooling heat exchanger and is used for forcibly exchanging heat for the steam after heat exchange of the dry quenching tank 14, the liquid of the main heat exchanger 13 is provided with the gas-liquid separator, and the steam outlet end of the main heat exchanger 13 is communicated with the steam inlet end of the outer pipe 32 and is used for introducing backflow steam.
Example 2
In this embodiment, the recycling device provided in embodiment 1 is used to recycle the condensate, and the specific implementation process is as follows:
step S1: introducing the heat tracing steam of the refining tank 11 and the loading and unloading station 15 into a buffer tank 17 of a recovery device for collection, and pressurizing the mixed heat tracing steam to 8bar through a pressurizing pump;
step S2: introducing the pressurized heat tracing steam into an inner pipe 31 of a cooling tower 12, introducing reflux steam into an outer pipe 32, gradually exchanging heat of the heat tracing steam and the reflux steam in the cooling tower 12, mixing the heat exchanging in a communicating pipeline to obtain primary cooling steam, and controlling the amount of the heat tracing reflux steam to control the temperature of the primary cooling steam to be 70 ℃ through a temperature sensor 22 and a pneumatic ball valve 23;
step S3: introducing the primary cooling steam into an auxiliary heat exchanger 16 for heat exchange and temperature reduction and gas-liquid separation to respectively obtain auxiliary condensate and final cooling steam, recycling the auxiliary condensate, controlling the temperature of the final cooling steam after heat exchange of the auxiliary heat exchanger 16 to be 40 ℃, then introducing the final cooling steam into an annular flue gas channel of the dry quenching tank 14, and cooling red coke in the dry quenching tank 14;
step S4: and the final cooling steam exchanges heat and rises temperature in the dry quenching tank 14, then is introduced into the main heat exchanger 13 to be cooled and subjected to gas-liquid separation, main condensate and reflux steam are respectively obtained, the main condensate is recycled, the temperature of the reflux steam after heat exchange of the main heat exchanger 13 is controlled to be 32 ℃, then the reflux steam is introduced into the outer pipe 32 of the cooling tower 12, the reflux steam and the heat tracing steam in the inner pipe 31 carry out heat convection, and the circulating condensation of the heat tracing steam is realized.
Example 3
In this embodiment, the recycling device provided in embodiment 1 is used to recycle the condensate, and the specific implementation process is as follows:
step S1: introducing the heat tracing steam of the refining tank 11 and the loading and unloading station 15 into a buffer tank 17 of a recovery device for collection, and pressurizing the mixed heat tracing steam to 12bar through a pressurizing pump;
step S2: introducing the pressurized heat tracing steam into an inner pipe 31 of a cooling tower 12, introducing reflux steam into an outer pipe 32, gradually exchanging heat of the heat tracing steam and the reflux steam in the cooling tower 12, mixing the heat exchanging in a communicating pipeline to obtain primary cooling steam, and controlling the amount of the heat tracing reflux steam to control the temperature of the primary cooling steam to be 80 ℃ through a temperature sensor 22 and a pneumatic ball valve 23;
step S3: introducing the primary cooling steam into an auxiliary heat exchanger 16 for heat exchange and temperature reduction and gas-liquid separation to respectively obtain auxiliary condensate and final cooling steam, recycling the auxiliary condensate, controlling the temperature of the final cooling steam subjected to heat exchange by the auxiliary heat exchanger 16 to be 50 ℃, introducing the final cooling steam into an annular flue gas passage of the dry quenching tank 14, and reducing the temperature of red coke in the dry quenching tank 14;
step S4: and the final cooling steam exchanges heat and rises temperature in the dry quenching tank 14, then is introduced into the main heat exchanger 13 to be cooled and subjected to gas-liquid separation, main condensate and reflux steam are respectively obtained, the main condensate is recycled, the temperature of the reflux steam after heat exchange of the main heat exchanger 13 is controlled to be 45 ℃, then the reflux steam is introduced into the outer pipe 32 of the cooling tower 12, the reflux steam and the heat tracing steam in the inner pipe 31 carry out heat convection, and the circulating condensation of the heat tracing steam is realized.
Comparative example 1
The comparative example is the existing condensate recovery method, and the technical scheme is as follows: the heat tracing steam of the refining tank 11 and the loading and unloading station 15 is communicated to a main steam outlet pipeline of the main heat exchanger 13 through pipelines, and is sent into a dry quenching tank 14 for cooling after being mixed.
The way of example 2, example 3 and comparative example 1 was used for condensate recovery and the noise during operation was tested:
example 2 and example 3 noise test point settings:
test point 1: the outer side of the middle part of the cooling tower 12 is 1 m;
test point 2: the outer sides of the pipeline joints at the steam outlet ends of the outer pipe 32 and the inner pipe 31 are 1 mm;
comparative example 1 noise test point setting:
test point 3: the outer side of the joint of the main steam outlet pipeline of the heat tracing steam and main heat exchanger 13 is 1 m.
Specific test data are shown in table 1:
TABLE 1
As can be seen from the data in Table 1, the noise of the recovery device provided by the invention is 53-63dB when the condensate is recovered, and the convective vibration of high-temperature steam and low-temperature steam is effectively improved.
In the description herein, references to the description of "one embodiment," "an example," "a specific example" or the like are intended to mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The foregoing is illustrative and explanatory only of the present invention, and it is intended that the present invention cover modifications, additions, or substitutions by those skilled in the art, without departing from the spirit of the invention or exceeding the scope of the claims.
Claims (6)
1. A method for recovering condensate is characterized by comprising the following steps:
step S1: introducing heat tracing steam of the refining tank (11) and the loading and unloading station (15) into a buffer tank (17) of a recovery device for collection and pressurization;
step S2: introducing the pressurized heat tracing steam into an inner pipe (31) of a cooling tower (12), and mixing the heat tracing steam and the reflux steam after heat exchange in the cooling tower (12) to obtain primary cooling steam;
step S3: introducing the primary cooling steam into an auxiliary heat exchanger (16) for heat exchange and temperature reduction and gas-liquid separation to respectively obtain auxiliary condensate and final cooling steam, recycling the auxiliary condensate, and introducing the final cooling steam into a dry quenching tank (14) for temperature reduction of red coke;
step S4: and the final cooling steam is subjected to heat exchange in a dry quenching tank (14), then is introduced into a main heat exchanger (13) for cooling and gas-liquid separation to respectively obtain main condensate and reflux steam, the main condensate is recycled, the reflux steam is introduced into an outer pipe (32) of a cooling tower (12), and the reflux steam and heat tracing steam in an inner pipe (31) carry out heat convection.
2. A condensate recovery method according to claim 1, characterized in that the pressure of the heat-tracing steam in the buffer tank (17) is increased to 8-12 bar.
3. A condensate recovery process according to claim 1, wherein the temperature of the primary cooling steam is in the range of 70-80 ℃.
4. A condensate recovery process according to claim 1, wherein the final cold steam temperature is in the range of 40-50 ℃.
5. A condensate recovery process according to claim 1, wherein the reflux steam has a temperature of 32-45 ℃.
6. The condensate recovery method according to claim 1, wherein the recovery device comprises a cooling tower (12) arranged among the refining tank (11), the dry quenching tank (14) and the loading and unloading station (15) and used for regulating and controlling gradual heat exchange between the heat tracing steam and the reflux steam, and a steam outlet end of the cooling tower is communicated with an auxiliary heat exchanger (16) and used for condensing the primary cold steam.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202210323410.4A CN114733223B (en) | 2022-03-29 | 2022-03-29 | Condensate recovery method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210323410.4A CN114733223B (en) | 2022-03-29 | 2022-03-29 | Condensate recovery method |
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| CN114733223A true CN114733223A (en) | 2022-07-12 |
| CN114733223B CN114733223B (en) | 2023-08-29 |
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202868667U (en) * | 2012-10-15 | 2013-04-10 | 中国石油化工股份有限公司湖北化肥分公司 | Steam condensate liquid recovery device |
| CN106139944A (en) * | 2016-08-29 | 2016-11-23 | 青岛康泰重工机械有限公司 | Steam mixer |
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2022
- 2022-03-29 CN CN202210323410.4A patent/CN114733223B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202868667U (en) * | 2012-10-15 | 2013-04-10 | 中国石油化工股份有限公司湖北化肥分公司 | Steam condensate liquid recovery device |
| CN106139944A (en) * | 2016-08-29 | 2016-11-23 | 青岛康泰重工机械有限公司 | Steam mixer |
Non-Patent Citations (1)
| Title |
|---|
| 陈婧;: "MTP装置蒸汽凝液回收系统工艺优化改造", 广州化工, no. 17 * |
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