CN112569618A - Reboiler system and steam feeding method thereof - Google Patents
Reboiler system and steam feeding method thereof Download PDFInfo
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- CN112569618A CN112569618A CN201910925564.9A CN201910925564A CN112569618A CN 112569618 A CN112569618 A CN 112569618A CN 201910925564 A CN201910925564 A CN 201910925564A CN 112569618 A CN112569618 A CN 112569618A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01B—BOILING; BOILING APPARATUS ; EVAPORATION; EVAPORATION APPARATUS
- B01B1/00—Boiling; Boiling apparatus for physical or chemical purposes ; Evaporation in general
- B01B1/005—Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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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
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Abstract
The invention belongs to the field of chemical industry, and particularly discloses a reboiler system and a steam feeding method thereof, wherein the reboiler system comprises: a steam desuperheating tower and a reboiler; a saturated steam outlet is arranged at the top of the steam desuperheating tower, a condensed water outlet is arranged at the bottom of the steam desuperheating tower, a condensed water inlet is arranged at the upper part of the steam desuperheating tower, and a superheated steam inlet is arranged at the middle part of the steam desuperheating tower; the reboiler is respectively provided with a fractionating tower material flow inlet, a fractionating tower material flow outlet, a heat source inlet and a heat source outlet; the saturated steam outlet is connected with the heat source inlet, and the condensed water inlet is connected with the heat source outlet; the fractionating tower material flow inlet is connected with the bottom of the fractionating tower, and the fractionating tower material flow outlet is connected with the lower part of the fractionating tower. The invention changes the process flow of the steam system by arranging the steam overheating tower, improves the operation condition of the reboiler, reduces the material standard of the reboiler, improves the heat transfer efficiency of the reboiler, and realizes the purposes of saving steam consumption and reducing equipment investment.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a reboiler system and a steam feeding method thereof.
Background
A reboiler is widely used in the fields of petroleum and petrochemical industry as a heat source device of a fractionating tower, and among reboilers of various heat source media, a reboiler using steam as a heat source is the most common.
According to the difference of the pressure grade and the amount of the water vapor as the heat source, the following process is generally adopted:
1. when the water vapor consumption is less and the pressure is lower, the simple reboiler flow shown in figure 1 is utilized, the water vapor as a heating medium is directly introduced into a heat source inlet of the reboiler through a pipeline, the superheated water vapor is cooled and condensed in the reboiler, the condensed water is discharged from the reboiler, and a regulating valve is arranged on a pipeline for discharging the condensed water to regulate the flow of the condensed water discharged from the reboiler so as to control the temperature of the material flow returned to the fractionating tower by the reboiler, thereby achieving the purpose of controlling the heat load of the reboiler;
2. when the water vapor consumption is large and the pressure is high, the reboiler process with the condensation water tank as shown in fig. 2 is utilized, and the difference between the process and the above process is that a special condensation water tank is arranged on a condensation water pipeline discharged from the reboiler, and the process specifically comprises the following steps: the steam as heating medium is directly introduced into the heat source inlet of the reboiler through the pipeline, in the reboiler, the superheated steam is cooled and condensed, the condensed water is discharged from the reboiler, a special condensed water tank is arranged on the pipeline from which the condensed water is discharged, the condensed water from the reboiler is collected, the bottom liquid level of the condensed water tank is controlled by adjusting the flow rate of the discharged condensed water, an adjusting valve is arranged on the steam inlet pipeline of the reboiler, the stream temperature of the reboiler returned to the fractionating tower is controlled by controlling the flow rate of the steam, and the purpose of controlling the heat load of the reboiler is further achieved.
At present, in the field of petroleum refining and petrochemical industry, water vapor as a heat source medium usually generates at a power station and is sent to users through a pipe network, the distances among the users are different, conditions (temperature and pressure) required by the users are different, and in order to meet the steam using requirements of different users at the same time and avoid condensation phenomenon in the conveying of the pipe network, the overheating degree of the steam is usually higher.
In this case, the inventors have found that there are two problems with the prior art steam reboiler scheme and control method: firstly, the steam temperature is too high, so that a carbon steel reboiler cannot be used, and the equipment investment is obviously increased; secondly, the superheated steam needs a certain area in the reboiler for desuperheating, which causes the heat transfer coefficient of the steam side film to be reduced, the heat exchange area of the reboiler to be enlarged, and the equipment investment to be increased.
Disclosure of Invention
In order to solve the problems in the flow and the control method of the conventional steam reboiler, the invention provides a reboiler system, which changes the process flow of a steam system by arranging a steam superheating tower, improves the operating conditions of the reboiler, realizes the purposes of reducing the material standard of the reboiler, improving the heat transfer efficiency of the reboiler and reducing the equipment investment.
To achieve the above object, an aspect of the present invention provides a reboiler system comprising: a steam desuperheating tower and a reboiler;
a saturated steam outlet is arranged at the top of the steam desuperheating tower, a condensed water outlet is arranged at the bottom of the steam desuperheating tower, a condensed water inlet is arranged at the upper part of the steam desuperheating tower, and a superheated steam inlet is arranged at the middle part of the steam desuperheating tower;
the reboiler is respectively provided with a fractionating tower material flow inlet, a fractionating tower material flow outlet, a heat source inlet and a heat source outlet;
the saturated steam outlet is connected with the heat source inlet through a pipeline, and the condensed water inlet is connected with the heat source outlet through a pipeline;
the fractionating tower material flow inlet is connected with the bottom of the fractionating tower, and the fractionating tower material flow outlet is connected with the lower part of the fractionating tower.
In the invention, the steam desuperheating tower is not strictly limited and can be a packed tower provided with a section of packing bed layer or a plate tower provided with a tower tray, and both the packing and the tower tray are used for desuperheating of superheated steam; the sensible heat released by superheated steam from superheating to saturation causes part of the condensed water to vaporize, also reaching the saturated state.
According to the present invention, preferably, the superheated steam inlet is connected to a superheated steam feed line, and the superheated steam feed line is provided with a regulating valve for controlling and regulating the pressure at the top of the steam-removing superheated tower, i.e. controlling and regulating the pressure and temperature of saturated steam, and further controlling and regulating the temperature of the stream returning to the fractionating tower in the reboiler, so as to control the heat load of the reboiler. The control system can be adjusted more reliably by providing such a cascade control loop.
Meanwhile, in the invention, preferably, the condensed water outlet is connected with a condensed water discharge pipeline, and the condensed water discharge pipeline is provided with an adjusting valve for controlling the liquid level at the bottom of the steam superheating tower.
According to the invention, the condensed water inlet is preferably arranged below the heat source outlet, and the height difference between the condensed water inlet and the heat source outlet enables the condensed water in the reboiler to flow back to the upper part of the steam desuperheating tower by means of gravity, so that no additional power equipment is required.
In the invention, the superheated steam of the heat source is converted into saturated steam, and the material of the reboiler is selected from carbon steel.
In the present invention, in order to make the superheated steam and the condensed water sufficiently contact, it is preferable that a condensed water distributor connected to the condensed water inlet and a steam distributor connected to the superheated steam inlet are provided inside the steam desuperheating tower.
In another aspect, the invention provides a reboiler steam feed process comprising:
the superheated steam directly enters a steam de-superheating tower to exchange heat with saturated steam condensate from a reboiler to enable the superheated steam to reach a saturated state, and then the saturated steam is led out from the top of the steam de-superheating tower and sent to the reboiler;
the saturated steam exchanges heat with the material from the bottom of the fractionating tower in the reboiler, and the condensed water of the saturated steam obtained by condensation is led out from the bottom of the reboiler and sent to the upper part of the steam desuperheating tower;
condensed water of the steam desuperheating tower is discharged from the bottom of the tower.
According to the invention, preferably, saturated steam condensate extracted from the bottom of the reboiler automatically flows into the upper part of the steam desuperheating tower through a pipeline to realize heat exchange with superheated steam rising from the lower part of the steam desuperheating tower.
The reboiler system of the present invention is applied to actual chemical production, which shows high advancement. The material flow condition of a reboiler at the bottom of a stable tower of a light hydrocarbon recovery device of a petrochemical enterprise is as follows: the flow rate is 573t/h, the temperature is 173-. As known in the art, the reboiler requires 3.7MPaG grade steam as the heat source, the operating temperature of the grade steam being 415 ℃ and the maximum temperature being 450 ℃; operating pressure 3.7MPaG, maximum operating pressure 3.9 MPaG. As shown in FIG. 2, the reboiler process with condensed water tank is adopted for process calculation, and the selected reboiler has a specification of phi 1000 × 6000 and an effective heat transfer area of 274m2The design temperature was 455 ℃ and the design pressure was 4.55 MPaG. As a result of the material selection, the reboiler was made of Cr-Mo steel and the process consumed 3.7MPaG steam 19136kg/h in total.
By adopting reboilers with the same specification and applying the reboiler flow shown in figure 4, the design temperature is 300 ℃, the design pressure is 3.2MPaG, the reboilers can meet the requirements by adopting carbon steel materials, the flow totally consumes 3.7MPaG steam 18180kg/h, and steam 956kg/h can be saved compared with the reboiler flow with the condensation water tank.
Therefore, by adopting the process of the reboiler, the material of the reboiler is reduced, the consumption of superheated steam is reduced, and the investment cost and the operation cost are saved.
The above calculation is performed for a given reboiler heat duty Q, which is calculated as shown in equation 1:
Q＝KA△Tm＝m(h1-h2) Formula (II)1
Wherein the content of the first and second substances,
q-heat duty of reboiler;
a, calculating the required heat exchange area;
k-heat transfer coefficient of reboiler;
△Tm-temperature difference of heat transfer of reboiler;
m is the flow rate of the heat source steam;
h1-enthalpy of the heat source steam;
h2-enthalpy of the condensed water.
After the heat load Q of the reboiler is determined, the heat transfer area A of the reboiler is obtained by calculating the heat transfer of the reboiler and hydraulics, wherein the heat transfer area A is Q/(K)△Tm). By adopting the prior art, such as the flow and control method shown in FIG. 2, the heat source conditions of the reboiler are fixed, the superheated steam temperature is 415 ℃, the superheated steam pressure is 3.7MPaG, under the conditions, the selected reboiler specification is calculated to be phi 1000 multiplied by 6000, and the effective heat transfer area is 274m2。
On the other hand, with the process of the present invention, given the heat duty of the reboiler, the conditions of the reboiler heat source are varied depending on the size of the reboiler heat transfer area. This is because, after the invention is adopted, the steam at the heat source inlet of the reboiler is saturated steam, the temperature and the pressure of the saturated steam are changed along with the difference of the heat transfer area of the reboiler, and the process of the invention also supports and can control and adjust the change.
The following tables 1-2 show the energy-saving effect of the invention compared with the prior art when different areas are selected:
table 1:
table 2:
as can be seen from tables 1-2, when the same reboiler specification and the same heat source are adopted, the amount of steam consumed by the reboiler system of the present invention is less, the operating conditions are milder, and the thermal efficiency is higher. The steam consumption under the heat exchange effective areas of different reboilers in the invention is compared, the statistical result is shown in figure 6, and as can be seen from figure 6, the larger the heat exchange area is, the less the superheated steam is consumed by adopting the process of the invention, and the more moderate the operating conditions of the heat source are.
Compared with the prior art, the invention has the following advantages:
(1) in the invention, the heat source of the reboiler is changed from superheated steam into saturated steam, the steam temperature is greatly reduced, the pressure is also reduced, and the design temperature and the pressure of the reboiler are reduced, so that the equipment cost is reduced.
(2) In the invention, saturated steam is adopted for heat exchange, and the coefficient of a heat transfer film is far higher than that of superheated steam, so that the heat transfer efficiency of the reboiler in unit area is improved, and more energy is saved.
(3) Based on the heat balance and heat transfer analysis of the reboiler system of the present invention, it is known that the larger the heat transfer area, the higher the heat transfer efficiency, and the lower the discharge temperature of the condensed water, the less the amount of steam consumed, and thus the more energy efficient, at a given reboiler heat load.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
Figure 1 shows a schematic of a prior art reboiler steam feed scheme.
Figure 2 shows a schematic of a prior art reboiler steam feed scheme.
FIG. 3 shows a schematic of the reboiler steam feed scheme in a comparative example of the invention.
FIG. 4 shows a schematic of the reboiler steam feed scheme in one particular embodiment of the present invention.
FIG. 5 shows a schematic of a steam desuperheating column in a specific embodiment of the invention.
FIG. 6 shows a schematic diagram of the consumption of superheated steam as it varies with the effective heat exchange area of the reboiler in one particular embodiment of the present invention.
Description of reference numerals:
1. a reboiler; 2. a fractionating column; 3. a steam desuperheating tower; 4. a condensed water distributor; 5. a filler; 6. a steam distributor; 7. a saturated steam outlet; 8. a condensate inlet; 9. a superheated steam inlet; 10. a condensed water outlet; 11. a condensation water tank.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
Example 1
This example serves to illustrate the reboiler system of the present invention comprising: a steam desuperheating tower 3 and a reboiler 1;
the steam desuperheating tower 3 is a carbon steel packed tower, a saturated steam outlet 7 is arranged at the top of the tower, a condensed water outlet 10 is arranged at the bottom of the tower, a condensed water inlet 8 is arranged at the upper part of the tower, and a superheated steam inlet 9 is arranged at the middle part of the tower; wherein, the superheated steam inlet 9 is connected with a superheated steam feeding pipeline, the superheated steam feeding pipeline is provided with a regulating valve for controlling the pressure at the top of the steam desuperheating tower 3, the condensed water outlet 10 is connected with a condensed water discharging pipeline, and the condensed water discharging pipeline is provided with a regulating valve for controlling the liquid level at the bottom of the steam desuperheating tower 3.
The upper part and the lower part of the packing in the steam-removing and superheating tower 3 (see figure 5) are respectively provided with a condensed water distributor 4 and a steam distributor 6, the condensed water distributor 4 is connected with a condensed water inlet 8, and the steam distributor 6 is connected with a superheated steam inlet 9.
The reboiler 1 is respectively provided with a fractionating tower material flow inlet, a fractionating tower material flow outlet, a heat source inlet and a heat source outlet; the shell diameter of the reboiler 1 was 1000mm and the tube length was 6000 mm.
The saturated steam outlet 7 is connected with a reboiler heat source inlet through a pipeline, and the condensed water inlet 8 is connected with a reboiler heat source outlet through a pipeline; the fractionating tower material flow inlet is connected with the bottom of the fractionating tower 2, and the fractionating tower material flow outlet is connected with the lower part of the fractionating tower 2. The condensed water inlet 8 is arranged below the heat source outlet, and the height difference between the condensed water inlet 8 and the heat source outlet enables the condensed water in the reboiler 1 to flow back to the upper part of the steam desuperheating tower 3 by means of gravity.
The steam feeding is carried out by adopting the reboiling system, and the feeding flow is shown in figure 4:
the superheated steam with the temperature of 415 ℃ and the pressure of 3.7MPaG enters a steam de-superheating tower, exchanges heat with saturated steam condensate from a reboiler to ensure that the superheated steam reaches a saturated state, and then is led out from the top of the steam de-superheating tower and sent to the reboiler;
the saturated steam exchanges heat with the material from the bottom of the fractionating tower in the reboiler, and condensed saturated steam condensate is led out from the bottom of the reboiler and sent to the upper part of the steam desuperheating tower;
condensed water in the steam desuperheating tower is discharged from the bottom of the tower, and the temperature of the condensed liquid is 224 ℃.
Comparative example 1
The reboiler system employed in this comparative example comprised: a condensation water tank 11 and a reboiler 1;
the reboiler 1 is made of 15CrMo and is respectively provided with a fractionating tower material flow inlet, a fractionating tower material flow outlet, a heat source inlet and a heat source outlet; the heat source inlet is connected with a superheated steam feeding pipeline, and the heat source outlet is connected with the upper part of the condensed water tank 11; a condensed water extraction pipeline is arranged at the bottom of the condensed water tank; the fractionating tower material flow inlet is connected with the bottom of the fractionating tower 2, and the fractionating tower material flow outlet is connected with the lower part of the fractionating tower 2.
The steam feeding is carried out by adopting the reboiling system, and the feeding flow is shown in figure 3:
superheated steam having a temperature of 415 ℃ and a pressure of 3.7MPaG is introduced into the reboiler 1 as a heat source to exchange heat with the material flow from the bottom of the fractionating tower 2, the material flow from the bottom of the fractionating tower 2 which has been heated and vaporized is returned to the fractionating tower, condensed water is introduced into the condensate tank 11 and discharged from the bottom of the condensate tank, and the temperature of the condensed water is 246 ℃.
The steam feed flow of the reboiling system of example 1 is compared with that of comparative example 1, and the results are shown in table 2:
TABLE 2
From the above, the reboiler system of comparative example 1 has two main problems:
1. the choice of reboiler material is too high because the superheated steam temperature from the pipe network is high (up to 415 ℃), leading to increased reboiler design conditions.
2. The heat transfer coefficient on the vapor side of the reboiler is low because the condensation of superheated vapor inside the reboiler is actually divided into two stages: the method comprises the following steps that firstly, superheated steam is desuperheated, heat exchange is started when the superheated steam enters a reboiler until the superheated steam is changed into saturated steam, the process is mainly a sensible heat release process of the superheated steam, and the heat transfer coefficient is low; ② the condensation of saturated steam, which is the release process of the latent heat of condensation of saturated steam, the heat transfer coefficient is larger, in comparative example 1, the total heat transfer coefficient on the steam side is not high due to the existence of the first stage.
In example 1, the superheated steam at 415 ℃ is reduced to the saturated steam at 224 ℃ by introducing the steam-removing superheated tower, so that the operating condition of the reboiler is improved,the material quality of the reboiler is reduced from 15CrMo to ordinary carbon steel, and the heat transfer coefficient of the steam side is 5807kcal/m2The h.DEG C is increased to 14918 kcal/square meter h.DEG C, thus realizing the purposes of reducing the material standard of the reboiler, improving the heat transfer efficiency of the reboiler and reducing the equipment investment.
In terms of economic and energy-saving benefits, after the process of the invention is adopted in the example 1, compared with the comparative example 1, the internal parts of the desuperheating tower are increased, and the investment is increased by about 25 ten thousand yuan; the material of the reboiler is reduced, the investment is reduced by about 10 ten thousand yuan, the superheated steam consumption is reduced by 956kg/h, and the annual operation cost can be saved by about 120 ten thousand yuan; the investment recovery period is within 0.5 year, the investment return is good, and the energy-saving effect is obvious.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (9)
1. A reboiler system characterized in that the reboiler system comprises: a steam desuperheating tower and a reboiler;
a saturated steam outlet is arranged at the top of the steam desuperheating tower, a condensed water outlet is arranged at the bottom of the steam desuperheating tower, a condensed water inlet is arranged at the upper part of the steam desuperheating tower, and a superheated steam inlet is arranged at the middle part of the steam desuperheating tower;
the reboiler is respectively provided with a fractionating tower material flow inlet, a fractionating tower material flow outlet, a heat source inlet and a heat source outlet;
the saturated steam outlet is connected with the heat source inlet through a pipeline, and the condensed water inlet is connected with the heat source outlet through a pipeline;
the fractionating tower material flow inlet is connected with the bottom of the fractionating tower, and the fractionating tower material flow outlet is connected with the lower part of the fractionating tower.
2. The reboiler system of claim 1 wherein the vapor desuperheating column is a packed column or a tray column.
3. The reboiler system of claim 1 wherein the superheated steam inlet is connected to a superheated steam feed line having a control valve to control the pressure at the top of the steam stripping column and thereby control the temperature of the reboiler stream returned to the fractionation column.
4. The reboiler system of claim 1 wherein a condensate drain line is connected to the condensate outlet and has a control valve for controlling the liquid level at the bottom of the vapor superheating column.
5. The reboiler system of claim 1 wherein the condensate inlet is disposed below the heat source outlet at a height differential such that condensate within the reboiler can flow back by gravity to an upper portion of the vapor desuperheating column.
6. The reboiler system of claim 1 wherein the reboiler is of carbon steel.
7. The reboiler system of claim 1 wherein said vapor desuperheating column is internally provided with a condensed water distributor connected to a condensed water inlet and a vapor distributor connected to a superheated vapor inlet.
8. A reboiler steam feed process, characterized in that the reboiler steam feed process comprises:
the superheated steam directly enters a steam de-superheating tower to exchange heat with saturated steam condensate from a reboiler to enable the superheated steam to reach a saturated state, and then the saturated steam is led out from the top of the steam de-superheating tower and sent to the reboiler;
the saturated steam exchanges heat with the material from the bottom of the fractionating tower in the reboiler, and the condensed water of the saturated steam obtained by condensation is led out from the bottom of the reboiler and sent to the upper part of the steam desuperheating tower;
condensed water at the bottom of the steam desuperheating tower is discharged from the bottom of the tower.
9. The reboiler steam feed process of claim 8 wherein saturated steam condensate exiting the bottom of the reboiler is piped from an upper portion of the steam desuperheating column to exchange heat with superheated steam rising from a lower portion of the steam desuperheating column.
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| WO2022241377A1 (en) * | 2021-05-11 | 2022-11-17 | Saudi Arabian Oil Company | Dynamic heating media conditioning for heat transfer optimization and fouling control |
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