CN204051035U - Utilize the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol - Google Patents
Utilize the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol Download PDFInfo
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- CN204051035U CN204051035U CN201420380141.6U CN201420380141U CN204051035U CN 204051035 U CN204051035 U CN 204051035U CN 201420380141 U CN201420380141 U CN 201420380141U CN 204051035 U CN204051035 U CN 204051035U
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Abstract
The utility model provides a kind of rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol, comprise the crude carbinol storage tank be connected successively, crude carbinol preheater, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, the first cooler be connected with pre-rectifying tower, be connected with atmospheric distillation tower second, 3rd cooler, the the first reformed gas separator be connected with compression rectification tower reboiler, the the second reformed gas separator be connected with pre-rectifying tower reboiler, it is characterized in that first, the condensate liquid of the second reformed gas separator is connected with crude carbinol preheater medium inlet by the first carrier pipe, crude carbinol preheater media outlet passes through the second carrier pipe respectively with first, second, 3rd cooler is connected.Take full advantage of the waste heat that temperature is the condensate liquid of 95 DEG C-115 DEG C, crude carbinol is preheated to the optimum temperature range of 65 DEG C ~ 70 DEG C, effectively reduces energy consumption, steady working condition, ensure that refined methanol product quality.
Description
Technical field
The utility model relates to a kind of rectifier unit, especially a kind of in the production process with coke-stove gas methyl alcohol, utilizes the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol, belongs to coking of coal byproduct production technical field.
Background technology
In three-tower rectification operation in methanol production, crude carbinol, before entering pre-rectifying tower, first will carry out preheating in crude carbinol preheater, thus after making the crude carbinol after preheating enter pre-rectifying tower, the thermal energy consumption of pre-rectifying tower tower reactor can be reduced, stablize pre-rectifying tower operating mode.Pressurizing tower qualified methyl alcohol is out sent in crude carbinol preheater by prior art mostly, carries out preheating to utilize the waste heat of qualified methyl alcohol to crude carbinol.In actual production, crude carbinol can only be preheated to 53 DEG C by the waste heat of qualified methyl alcohol, do not reach the best feeding temperature requirement of the crude carbinol of 65 DEG C ~ 70 DEG C far away, this will increase the thermal source energy consumption of pre-rectifying tower tower reactor, and feeding temperature fluctuation causes indices in pre-rectifying tower unstable, is unfavorable for the long-term low consumption stable operation of pre-rectifying tower.In addition, the reformed gas that the reboiler of existing rectifying column is mostly come with conversion section is for thermal source, and return conversion section again after heat exchange, after heat exchange, isolated condensate temperature is about 95 DEG C-115 DEG C, this part heat energy does not utilize and just directly drains into recirculated water pipe network, causes a large amount of heat-energy losses.Therefore, must to prior art Optimal improvements in addition, to make full use of this part heat energy of condensate liquid.
Summary of the invention
Carry out preheating for making full use of reformed gas condensate liquid waste heat to the crude carbinol entering pre-rectifying tower, reduce operating mode in pre-rectifying tower energy consumption, stabilizer, the utility model provides a kind of rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol.
The utility model is completed by following technical proposal: a kind of rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol, comprise the crude carbinol storage tank be connected successively, crude carbinol preheater, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, the first cooler be connected with pre-rectifying tower, be connected with atmospheric distillation tower second, 3rd cooler, the the first reformed gas separator be connected with compression rectification tower reboiler, the the second reformed gas separator be connected with pre-rectifying tower reboiler, it is characterized in that first, the condensate liquid of the second reformed gas separator is connected with crude carbinol preheater medium inlet by the first carrier pipe, crude carbinol preheater media outlet passes through the second carrier pipe respectively with first, second, 3rd cooler is connected, send in crude carbinol preheater with condensate liquid temperature being reached 95 DEG C-115 DEG C through the first carrier pipe, the waste heat of condensate liquid is utilized to carry out preheating to crude carbinol, the temperature of crude carbinol is effectively increased to the optimum temperature range of 65 DEG C ~ 70 DEG C, reduce pre-rectifying tower energy consumption, steady working condition, condensate liquid simultaneously after preheating through the second carrier pipe respectively to first, second, 3rd cooler moisturizing.
Described second carrier pipe is set to the first arm, the second arm and the 3rd arm respectively, wherein the first arm is connected with the first cooler, second arm is connected with the second cooler, 3rd arm is connected with the 3rd cooler, with by with crude carbinol carry out the condensate liquid after heat exchange respectively through first, second, third arm to corresponding cooler moisturizing.
Described first reformed gas separator is connected with compression rectification tower reboiler media outlet by pipeline, the reformed gas carrier pipe that this reboiler medium inlet and conversion section are come is connected, first reformed gas separator gas outlet is connected with pre-rectifying tower reboiler medium inlet by pipeline, first reformed gas separator condensate outlet is connected with crude carbinol preheater medium inlet by the first carrier pipe, the reformed gas after heat exchange is sent in the first reformed gas separator, isolated reformed gas is made to continue to send pre-rectifying tower reboiler to carry out heat exchange again, and the condensate liquid that isolated temperature is 95 DEG C-115 DEG C sends into preheating crude carbinol in crude carbinol preheater through the first carrier pipe.
Described second reformed gas separator is connected with pre-rectifying tower reboiler media outlet by pipeline, second reformed gas separator gas outlet send conversion procedure by pipeline, second reformed gas separator condensate outlet is connected with crude carbinol preheater medium inlet by pipeline first carrier pipe, the second reformed gas separator is entered after making the isolated reformed gas of the first conversion separator continue to send pre-rectifying tower reboiler to carry out heat exchange again, so that isolated reformed gas is sent into conversion procedure recycling, and the condensate liquid that isolated temperature is 95 DEG C-115 DEG C sends into preheating crude carbinol in crude carbinol preheater through the first carrier pipe.
The utility model has following advantages and effect: adopt such scheme, the condensate liquid that temperature can be reached 95 DEG C-115 DEG C is sent in crude carbinol preheater through the first carrier pipe, the waste heat taking full advantage of condensate liquid carries out preheating to crude carbinol, the temperature of crude carbinol is effectively increased to the optimum temperature range of 65 DEG C ~ 70 DEG C, effective reduction pre-rectifying tower energy consumption, steady working condition, and provide safeguard for the methanol rectification quality of postorder, ensure that refined methanol product quality, condensate liquid simultaneously after preheating through the second carrier pipe respectively to first, second, 3rd cooler moisturizing, for manufacturing enterprise creates larger profit margin.
Accompanying drawing explanation
Fig. 1 is the utility model structural representation.
In figure, 1 is the first cooler, and 2 is the first arm, 3 is pre-rectifying tower, and 4 is crude carbinol preheater, and 5 is the first carrier pipe, 6 is crude carbinol storage tank, and 7 is the second arm, and 8 is pre-rectifying tower reboiler, 9 is the second reformed gas separator, and 10 is the second cooler, and 11 is refined methanol storage tank, 12 is the 3rd cooler, and 13 is atmospheric distillation tower, and 14 is compression rectification tower, 15 is compression rectification tower reboiler, the 16 reformed gas carrier pipes of coming for conversion section, and 17 is the first reformed gas separator.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described further.
The rectifier unit of what the utility model provided utilize reformed gas condensate liquid waste-heat crude carbinol, comprise the crude carbinol storage tank 6 be connected successively, crude carbinol preheater 4, pre-rectifying tower 3, compression rectification tower 14, atmospheric distillation tower 13, the first cooler 1 be connected with pre-rectifying tower 3, be connected with atmospheric distillation tower 13 second, 3rd cooler 10 and 12, the the first reformed gas separator 17 be connected with compression rectification tower 14 reboiler 15, the the second reformed gas separator 9 be connected with pre-rectifying tower 3 reboiler 8, first, second reformed gas separator 17, the condensate liquid of 9 is connected with crude carbinol preheater 4 medium inlet by the first carrier pipe 5, crude carbinol preheater 4 media outlet passes through the second carrier pipe respectively with first, second, 3rd cooler 1, 10, 12 are connected, described second carrier pipe is set to the first arm 2, second arm 7 and the 3rd arm 18 respectively, wherein the first arm 2 is connected with the first cooler 1, second arm 7 is connected with the second cooler 10,3rd arm 17 is connected with the 3rd cooler 12, with by with crude carbinol carry out in crude carbinol preheater 4 condensate liquid after heat exchange respectively through first, second, third arm 2,7,18 to corresponding cooler 1,10,12 moisturizing, described first reformed gas separator 17 is connected with compression rectification tower 14 reboiler 15 media outlet by pipeline, this reboiler 15 medium inlet is connected with the reformed gas carrier pipe 16 that conversion section is come, first reformed gas separator 17 gas vent is connected with pre-rectifying tower 3 reboiler 8 medium inlet by pipeline, first reformed gas separator 17 condensate outlet is connected with crude carbinol preheater 4 medium inlet by the first carrier pipe 5, so that the reformed gas after reboiler 15 heat exchange is sent in the first reformed gas separator 17, isolated reformed gas is made to continue to send pre-rectifying tower 3 reboiler 8 to carry out heat exchange again, and the condensate liquid that isolated temperature is 95 DEG C-115 DEG C sends into preheating crude carbinol in crude carbinol preheater 4 through the first carrier pipe 5, described second reformed gas separator 9 is connected with pre-rectifying tower 3 reboiler 8 media outlet by pipeline, second reformed gas separator 9 gas vent send conversion procedure by pipeline, second reformed gas separator 9 condensate outlet is connected with crude carbinol preheater 4 medium inlet by the first carrier pipe 5, the second reformed gas separator 9 is entered after making the isolated reformed gas of the first conversion separator 17 continue to send pre-rectifying tower 3 reboiler 8 to carry out heat exchange again, so that isolated reformed gas is sent into conversion procedure recycling, and the condensate liquid that isolated temperature is 95 DEG C-115 DEG C sends into preheating crude carbinol in crude carbinol preheater 4 through the first carrier pipe 5, to make full use of the condensate liquid waste heat that temperature is 95 DEG C-115 DEG C, reduce energy consumption.
Claims (4)
1. one kind utilizes the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol, comprise the crude carbinol storage tank be connected successively, crude carbinol preheater, pre-rectifying tower, compression rectification tower, atmospheric distillation tower, the first cooler be connected with pre-rectifying tower, be connected with atmospheric distillation tower second, 3rd cooler, the the first reformed gas separator be connected with compression rectification tower reboiler, the the second reformed gas separator be connected with pre-rectifying tower reboiler, it is characterized in that first, the condensate liquid of the second reformed gas separator is connected with crude carbinol preheater medium inlet by the first carrier pipe, crude carbinol preheater media outlet passes through the second carrier pipe respectively with first, second, 3rd cooler is connected.
2. the rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol according to claim 1, it is characterized in that described second carrier pipe is set to the first arm, the second arm and the 3rd arm respectively, wherein the first arm is connected with the first cooler, second arm is connected with the second cooler, and the 3rd arm is connected with the 3rd cooler.
3. the rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol according to claim 1, it is characterized in that described first reformed gas separator is connected with compression rectification tower reboiler media outlet by pipeline, the reformed gas carrier pipe that this reboiler medium inlet and conversion section are come is connected, first reformed gas separator gas outlet is connected with pre-rectifying tower reboiler medium inlet by pipeline, and the first reformed gas separator condensate outlet is connected with crude carbinol preheater medium inlet by the first carrier pipe.
4. the rectifier unit utilizing reformed gas condensate liquid waste-heat crude carbinol according to claim 1, it is characterized in that described second reformed gas separator is connected with pre-rectifying tower reboiler media outlet by pipeline, second reformed gas separator gas outlet send conversion procedure by pipeline, and the second reformed gas separator condensate outlet is connected with crude carbinol preheater medium inlet by pipeline first carrier pipe.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420380141.6U CN204051035U (en) | 2014-07-10 | 2014-07-10 | Utilize the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol |
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| CN201420380141.6U CN204051035U (en) | 2014-07-10 | 2014-07-10 | Utilize the rectifier unit of reformed gas condensate liquid waste-heat crude carbinol |
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| CN204051035U true CN204051035U (en) | 2014-12-31 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104710281A (en) * | 2015-03-18 | 2015-06-17 | 四川天一科技股份有限公司 | Methanol pre-rectifying tower heating process by utilizing methanol synthetic reaction gas |
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2014
- 2014-07-10 CN CN201420380141.6U patent/CN204051035U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104710281A (en) * | 2015-03-18 | 2015-06-17 | 四川天一科技股份有限公司 | Methanol pre-rectifying tower heating process by utilizing methanol synthetic reaction gas |
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