CN210419230U - Conversion system for preparing methanol by coal gasification - Google Patents
Conversion system for preparing methanol by coal gasification Download PDFInfo
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- CN210419230U CN210419230U CN201921426934.6U CN201921426934U CN210419230U CN 210419230 U CN210419230 U CN 210419230U CN 201921426934 U CN201921426934 U CN 201921426934U CN 210419230 U CN210419230 U CN 210419230U
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Abstract
The utility model belongs to the technical field of coal chemical industry, and relates to a methanol conversion system by coal gasification, which comprises a separator, a detoxification tank, a conversion furnace and a steam superheater; the top outlet of the separator is divided into two branches, wherein one branch is the top outlet of the separator and is connected with the shell pass inlet of the conversion furnace through a detoxification groove; the shell pass outlet of the shift converter is divided into two branches, wherein one branch is connected with the shell pass inlet of the steam superheater; the coal gasification methanol conversion system also comprises a first steam pipeline and a second steam pipeline, wherein the first steam pipeline is connected with a shell pass inlet of the conversion furnace; the second steam pipeline is respectively connected with a tube pass inlet of the shift converter and a tube pass inlet of the steam superheater; a valve is also arranged on the first steam pipeline. The utility model discloses the heat utilization is reasonable, and catalyst activity is good, longe-lived, and processing equipment is simple, and transform system operation is stable.
Description
Technical Field
The utility model belongs to the technical field of the coal chemical industry, a coal gasification system methyl alcohol transform system is related to.
Background
In the methanol synthesis, the shift process refers to a process of carrying out a chemical reaction on raw gas and water vapor at a certain temperature by virtue of the action of a catalyst to generate carbon dioxide and hydrogen by carbon monoxide. The carbon monoxide in the crude gas is removed through the shift reaction, and the methanol synthesis gas is obtained, so the shift process is a conversion process and a purification process in the methanol synthesis.
When the coal is gasified to prepare a product, when the raw gas has a high steam-gas ratio, if the raw gas with high CO content and low pressure and the raw gas with low CO content and high pressure are shifted to prepare methanol, the following problems are caused: the bed temperature of the catalyst is high and is difficult to control, so that the activity of the catalyst is poor; the system has unreasonable heat utilization rate and low heat utilization rate, and the adopted conversion process is different due to different CO content and pressure, and the process is more complex.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems of unreasonable heat utilization, poor catalyst activity and complex process in the background technology, the utility model provides a shift system for preparing methanol by coal gasification, which has the advantages of reasonable heat utilization, good catalyst activity, long service life, simple process equipment, stable shift system operation and wide application range.
In order to realize the purpose, the utility model discloses a technical scheme be:
a coal gasification system methanol conversion system which is characterized in that: the coal gasification methanol conversion system comprises a separator (1), a detoxification tank, a conversion furnace and a steam superheater;
the separator is provided with an inlet, a top outlet and a bottom outlet; the shift converter and the steam superheater are respectively provided with a shell pass inlet, a shell pass outlet, a tube pass inlet and a tube pass outlet;
the top outlet of the separator is divided into two branches, wherein one branch is the top outlet of the separator and is connected with the shell pass inlet of the conversion furnace through a detoxification groove; the shell-side outlet of the shift converter is divided into two branches, wherein one branch is connected with the shell-side inlet of the steam superheater.
Further, the coal gasification methanol conversion system also comprises a first steam pipeline and a second steam pipeline, wherein the first steam pipeline is connected with a shell pass inlet of the conversion furnace; and the second steam pipeline is respectively connected with a tube pass inlet of the shift converter and a tube pass inlet of the steam superheater.
Furthermore, a valve is arranged on the first steam pipeline.
Furthermore, the coal gasification methanol conversion system also comprises a heat exchanger, and an outlet at the top of the separator is connected with an inlet of the detoxification tank through the heat exchanger; and the other branch of the shell pass outlet of the shift converter is connected with the heat exchanger.
Further, the shift converter is a spiral tube type shift converter, and the steam superheater is a spiral tube type steam superheater.
Further limiting, a catalyst bed layer is arranged in the shell side of the shift converter.
Further defined, the catalyst bed is a sulfur tolerant shift catalyst bed.
The utility model has the advantages that:
1. the utility model provides a conversion system for preparing methanol by coal gasification, which comprises a separator, a detoxification tank, a conversion furnace and a steam superheater; the top outlet of the separator is divided into two branches, wherein one branch is the top outlet of the separator and is connected with the shell pass inlet of the conversion furnace through the detoxification groove; the shell pass outlet of the shift converter is divided into two branches, wherein one branch is connected with the shell pass inlet of the steam superheater; the utility model provides a transform technology heat utilizes rationally, and equipment is simple, easy operation and with low costs.
2. The coal gasification methanol conversion system provided by the utility model also comprises a first steam pipeline and a second steam pipeline, wherein the first steam pipeline is connected with the shell pass inlet of the conversion furnace; the second steam pipeline is respectively connected with a tube pass inlet of the shift converter and a tube pass inlet of the steam superheater; a valve is also arranged on the first steam pipeline. When the ratio of the steam to the gas of the gasified crude coal is 0.6-0.9, the pressure is low and the content of CO is high, opening a valve on a first steam pipeline, and introducing saturated steam of the first steam pipeline into the shell pass of the shift converter from the first steam pipeline; the pressure of saturated steam flowing into the first steam pipeline is slightly greater than the pressure of the gasified crude gas, so that the crude gas flowing into the conversion furnace is prevented from generating dew point and the conversion effect is prevented from being influenced; the saturated steam part of the second steam pipeline enters the tube pass of the shift converter to exchange and transfer reaction heat in the shell pass of the shift converter, so that the bed temperature of the catalyst is reduced, the temperature in the shift converter is ensured to be within the catalyst operating temperature range, and the service life of the catalyst is prolonged; and the heat exchange effect is good, and the system heat utilization is reasonable.
3. The utility model discloses the transform furnace is spiral tubular transform furnace, is provided with the catalyst bed in the transform furnace shell side, and the catalyst bed is sulfur-tolerant catalyst bed, and when the raw coal gas in the technology was changeed in the transform furnace, the reactivity of catalyst was good, and the transform reaction can go on smoothly, and transform efficiency is good.
Drawings
FIG. 1 is a schematic view of a process flow of a shift system for producing methanol by coal gasification according to the present invention;
wherein:
1-a separator; 2-a detoxification tank; 3-a shift converter; 4-steam superheater; 5, a heat exchanger; 6, a valve.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings and embodiments.
Example 1
Referring to fig. 1, the utility model provides a coal gasification system methanol conversion system, including separator 1, heat exchanger 5, detoxify groove 2, shift converter 3, steam over heater 4, first steam conduit and second steam conduit.
Specifically, raw coal gas from coal gasification is connected with an inlet of a separator 1; an outlet at the bottom end of the separator 1 is connected to a system waste liquid pipe network; the outlet at the top end of the separator 1 comprises two branches; one branch is that the outlet at the top end of the separator 1 is connected with the inlet of the detoxification tank 2 through a heat exchanger 5; the other branch is a system after the top outlet of the separator 1 directly enters the conversion; an outlet of the detoxification tank 2 is connected with a shell pass inlet of the shift converter 3, a valve 6 is arranged on the first steam pipeline, and the valve 6 can adjust the pressure of saturated steam flowing through the first steam pipeline; specifically, the valve 6 can be a self-operated pressure regulating valve commonly used in industry; the shell pass outlet of the shift converter 3 is divided into two branches, one branch is that the shell pass outlet of the shift converter 3 is connected with the shell pass inlet of the steam superheater 4, and the other branch is that the shell pass outlet of the shift converter 3 is sent into a post-shift system through a heat exchanger 5; a tube pass inlet of the shift converter 3 is connected with part of saturated steam from the second steam pipeline, and a tube pass outlet of the shift converter 3 is connected to the superheated steam pipe network; the shell side outlet of the steam superheater 4 is sent to a post-conversion system; the system is the system for making methanol after the transformation, and the top outlet of the steam superheater 4 tube side and the tube side outlet of the transformation furnace 3 are sent to the superheated steam pipe network together, and the bottom inlet of the steam superheater 4 tube side is mixed with the saturated steam from the second steam pipeline and the steam from the methanol synthesis and then enters the tube side of the steam superheater 4 for heat exchange in the transformed process gas, so that the heat of the system is effectively utilized. When the method is implemented, the saturated steam in the first steam pipeline is 3.2-5.0 Mpa saturated steam; the saturated steam in the second steam line was 2.5Mpa saturated steam.
Example 2
In the implementation, because the pressure of the raw gas is low and the content of CO is high, in order to improve the efficiency of the conversion reaction, the heat utilization is reasonable, so that saturated steam is supplemented into the gas entering the conversion furnace, and before the conversion process is started, the valve 6 on the first steam pipeline needs to be opened. During implementation, the pressure of the supplemented saturated steam is slightly greater than that of the crude gas entering the conversion system, so that the saturated steam can be well and quickly supplemented into the crude gas, and meanwhile, the phenomenon that water vapor in the crude gas is increased due to leakage points to influence the conversion reaction is avoided.
Specifically, when the content of CO in the raw gas is 60 to 80% and the pressure is 3.0 to 4.5Mpa, a stream of saturated steam needs to be supplemented into the raw gas to achieve the conversion effect because the pressure of the raw gas is low and the content of CO is high, and the supplemented saturated steam pressure is slightly higher than the pressure of the raw gas to prevent the dew point from influencing the conversion effect, so that the heat utilization is reasonable and the conversion efficiency is better. Therefore, when the steam-gas ratio of the gasified crude coal gas is 0.6-0.9, the pressure is 3.0-4.5Mpa and the content of CO is 60-80%, opening a valve on the first steam pipeline, and introducing 3.2-5.0 Mpa saturated steam from the outside of the pipe into the shell pass of the shift converter from the first steam pipeline; and when the content of CO in the raw gas is 35-45% and the pressure is 5.5-6.5Mpa, saturated steam is not needed to be supplemented into the raw gas, and the valve on the first steam pipeline is closed when the process is implemented.
Example 3
The utility model discloses well converter 3 is spiral pipe heat transfer formula transform stove, and steam over heater 4's structure is the spiral tube formula, is provided with the catalyst bed in the transform furnace shell side, and the catalyst bed is resistant sulphur transform catalyst bed. Specifically, the catalyst can be B8-11 or QDB-04 type catalyst, and the operation temperature of the catalyst is low, generally 180-330 ℃; the carbon monoxide is lower after the conversion; strong sulfur toxicity resistance, good activity during transformation and high transformation efficiency.
Example 4
The conversion method of the conversion system provided by the utility model is described by taking the raw gas conversion with the steam-gas ratio of 0.8, the CO content of 60% and the pressure of 3.8MPa after coal gasification as an example. Because the pressure of the raw gas is lower and the content of CO is higher, in order to improve the efficiency of the shift reaction, the heat utilization is reasonable, therefore, before the shift process starts, the valve 6 on the first steam pipeline needs to be opened, and the pressure of the saturated steam entering the first saturated pipeline is 4.0 Mpa.
Referring to fig. 1, the specific transformation method flow is: after coal-water separation is carried out on the crude coal gas from coal gasification through a separator, the crude coal gas is divided into two branches to flow out from an outlet at the top of the separator, and part of the separated crude coal gas directly enters a conversion follow-up system to prepare methanol; part of the separated raw gas enters a detoxification tank 2 to remove impurities and heavy metals after heat exchange through a heat exchanger 5 from an outlet at the top end of a separator 1, the process gas is mixed with 4.0Mpa saturated steam and then enters a shell pass of a shift converter, and shift reaction CO + H is carried out in the shift converter 3 under the action of a catalyst B8-112O＝CO2+H2+ Q, the temperature of the catalyst bed is 230 ℃, because the shift reaction is an exothermic reaction, 2.5Mpa saturated steam is introduced from top to bottom in the tube pass of the shift converter 3, the heat generated by the shift reaction can be removed, the temperature of the shift converter bed is reduced, the service life of the catalyst is prolonged, and the activity of the catalyst is improved, therefore, the 2.5Mpa saturated steam entering the top end inlet of the tube pass of the shift converter 3 becomes 2.5Mpa superheated steam after heat exchange, and is sent to a system steam pipe network through the outlet at the bottom end of the tube pass of the shift converter 3; after the process gas completes CO conversion in the shell pass of the shift converter 3, the CO content in the process gas after conversion is 3 percent, and H content in the process gas after conversion is H2The volume ratio to CO was 2.15; therefore, the converted process gas is discharged from a shell pass outlet at the bottom end of the conversion furnace 3 and is divided into two branches, one branch enters a converted system for methanol preparation after heat recovery through the steam superheater 4, the other branch is also sent to the converted system for methanol preparation after heat exchange through the heat exchanger 5, the converted heat can preheat crude gas separated by coal water through the separator 1 through the heat exchanger 5, and the heat utilization is reasonable.
Example 5
Different from the embodiment 4, the steam-gas ratio of the raw gas is 0.6, the content of CO is 80%, the pressure of the raw gas is 3.0MPa, and the pressure of the raw gas is lower and the content of CO is higher, so that the conversion reaction efficiency is improved, the heat utilization is reasonable, the saturated steam is supplemented into the gas entering the converter 3, before the conversion process is started, the valve 6 on the first steam pipeline needs to be opened, and the pressure of the saturated steam supplemented from the first steam pipeline is 3.2 MPa.
During the shift reaction, in the shift furnace 3, the catalyst QDB-04 and the catalyst bed layer temperature are 280 deg.c, the catalyst has high activity, CO content in the shifted process gas is 4%, and H content is2The volume ratio of the gas to CO is 2.1, the requirement of the methanol preparation process is met, and the converted gas is sent to the methanol preparation process after heat recovery; the conversion efficiency is high, the whole system runs stably, and the heat efficiency is good.
Example 6
Different from the example 5, the steam-gas ratio of the raw gas is 0.9, the CO content is 70 percent, and the pressure of the raw gas is 4.5 MPa. Because the pressure of the raw gas is lower and the content of CO is higher, in order to improve the efficiency of the shift reaction and reasonably utilize heat, saturated steam is supplemented into the gas entering the shift converter 3, before the shift process starts, a valve 6 on a first steam pipeline needs to be opened, and the pressure of the supplemented saturated steam is 5.0 Mpa.
During the shift reaction, in the shift furnace 3, the catalyst QDB-04 and the catalyst bed temperature are 330 ℃, the catalyst activity is good, the CO content in the shifted process gas is 5 percent, and H is high2The volume ratio of the gas to CO is 2.05, the requirement of the methanol preparation process is met, and the converted gas is sent to the methanol preparation process after heat recovery; the CO conversion is good, the heat efficiency of the system is reasonably utilized, and the service life of the catalyst is prolonged.
Example 7
Different from the embodiment 3, the raw gas to be shifted has the steam-gas ratio of 0.8, the CO content of 40 percent and the pressure of 6.2MPa, and the gas entering the shift converter 3 does not need to be supplemented with gas because the pressure of the raw gas is higher and the CO content is lower, so the process closes the valve 6 on the first steam pipeline before shifting is started.
The specific conversion process flow is that the crude gas enters the shell pass of a shift converter 3 after coal water separation, the shift reaction is carried out in the shift converter 3 under the action of a B8-11 catalyst, the temperature of a catalyst bed layer is 265 ℃, because the shift reaction is an exothermic reaction, in order to ensure that the temperature of the catalyst bed layer is 265 ℃, 2.5Mpa saturated saturation is introduced into the tube pass of the shift converter 3 from top to bottomThe steam can remove the heat generated by the shift reaction, prolong the service life of the catalyst, improve the activity of the catalyst, and change 2.5Mpa saturated steam into 2.5Mpa superheated steam after heat exchange at the top end of the tube pass of the shift converter 3 and send the superheated steam to a system steam pipe network through the outlet at the bottom end of the tube pass of the shift converter 3; after the process gas completes CO conversion in the shell pass of the shift converter 3, the CO content in the process gas after conversion is 4.5 percent, and H content in the process gas after conversion is H2The volume ratio to CO is 2.08; therefore, the converted process gas is discharged from a shell pass outlet at the bottom end of the conversion furnace 3, heat recovery is carried out through the steam superheater 4 or the heat exchanger 5 respectively, and then the process gas enters a methanol preparation system after conversion, the converted heat can preheat the process gas separated by coal water through the separator 1, and the heat utilization is reasonable.
Example 8
Different from the embodiment 7, the raw gas to be shifted has the steam-gas ratio of 0.9, the CO content of 35 percent and the pressure of 5.5MPa, and the gas entering the shift converter does not need to be supplemented with gas because the pressure of the raw gas is higher and the CO content is lower, so the process closes the valve 6 on the first steam pipeline before shifting is started.
In the shift converter 3, the catalyst is QDB-04, the temperature of the catalyst bed is 300 ℃, the temperature of the catalyst bed is low, the catalyst cannot be damaged, the service life is prolonged, the shift reaction can be well promoted, the CO can be quickly shifted, the CO content in the process gas after the shift is 3.5 percent, and H is H2The volume ratio of the process gas to CO is 2.16, the converted process gas enters a methanol preparation system after conversion after being subjected to heat recovery through a steam superheater 4 or a heat exchanger 5, the whole conversion system is stable, and the heat efficiency is reasonably utilized.
Example 9
Different from the embodiment 7, the raw gas to be shifted has the steam-gas ratio of 0.6, the CO content of 45 percent and the pressure of 6.5MPa, and the gas entering the shift converter 3 does not need to be supplemented with gas because the pressure of the raw gas is higher and the CO content is lower, so the process closes the valve 6 on the first steam pipeline before shifting is started.
In the shift converter 3, the catalyst is B8-11, the temperature of the catalyst bed is 230 ℃, the temperature of the catalyst bed is low, and the catalyst is used for a long timeThe period is prolonged, the activity of the catalyst is good, the CO transformation reaction is accelerated, the CO content in the transformed process gas is 4 percent, and H is2The volume ratio of the process gas to CO is 2.05, the converted process gas enters a methanol preparation system after conversion after heat recovery through a steam superheater 4 or a heat exchanger 5, the conversion process is stable in operation, and the high-level heat of the system is well utilized.
Claims (7)
1. A coal gasification system methanol conversion system which is characterized in that: the coal gasification methanol conversion system comprises a separator (1), a detoxification tank (2), a conversion furnace (3) and a steam superheater (4);
the separator (1) is provided with an inlet, a top outlet and a bottom outlet; the shift converter (3) and the steam superheater (4) are respectively provided with a shell pass inlet, a shell pass outlet, a tube pass inlet and a tube pass outlet;
the top outlet of the separator (1) is divided into two branches, wherein one branch is the top outlet of the separator (1) and is connected with the shell-side inlet of the shift converter (3) through the detoxification groove (2); the shell-side outlet of the shift converter (3) is divided into two branches, wherein one branch is connected with the shell-side inlet of the steam superheater (4).
2. The coal gasification methanol conversion system according to claim 1, characterized in that: the coal gasification methanol conversion system also comprises a first steam pipeline and a second steam pipeline, wherein the first steam pipeline is connected with a shell pass inlet of the conversion furnace (3); and the second steam pipeline is respectively connected with a tube side inlet of the shift converter (3) and a tube side inlet of the steam superheater (4).
3. The coal gasification methanol conversion system according to claim 2, characterized in that: and a valve (6) is also arranged on the first steam pipeline.
4. The coal gasification methanol conversion system according to claim 1, 2, or 3, characterized in that: the coal gasification methanol conversion system also comprises a heat exchanger (5), and the top outlet of the separator (1) is connected with the inlet of the detoxification tank (2) through the heat exchanger (5); and the other branch of the shell pass outlet of the shift converter (3) is connected with a heat exchanger (5).
5. The coal gasification methanol conversion system according to claim 4, characterized in that: the shift converter (3) is a spiral tube type shift converter, and the steam superheater (4) is a spiral tube type steam superheater.
6. The coal gasification methanol conversion system according to claim 5, characterized in that: and a catalyst bed layer is arranged in the shell side of the shift converter (3).
7. The coal gasification methanol conversion system according to claim 6, characterized in that: the catalyst bed layer is a sulfur-tolerant shift catalyst bed layer.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110357040A (en) * | 2019-08-29 | 2019-10-22 | 陕西聚能新创煤化科技有限公司 | Coal gasification methanol transformation system and transform method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110357040A (en) * | 2019-08-29 | 2019-10-22 | 陕西聚能新创煤化科技有限公司 | Coal gasification methanol transformation system and transform method |
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