CN108558593B - Energy-saving process method for recovering butane in mixed C4 - Google Patents
Energy-saving process method for recovering butane in mixed C4 Download PDFInfo
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- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
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Abstract
The invention relates to an energy-saving process method for recovering butane in mixed C4. The raw material is pretreated by an alkane and alkene crude separation tower T101, and the bottom of the T101 exchanges heat between the tower bottom material and a high-temperature extracting agent extracted from the bottom of an extracting agent recovery tower IIT 105 by a heat exchanger E101. The extractive distillation column T102 uses an intermediate reboiler E201 to exchange heat with the high-temperature extractant extracted from the bottom of the extractant recovery column IIT 105. And adding an upper extractive distillation tower T103, and heating an upper extractive distillation tower T103 kettle reboiler E301 by extracting a gas phase from the top of an upper extractive distillation tower II. Through heat integration, not only can the separation of olefin and alkane be realized, but also the heat of different tastes in the butane recovery process is fully utilized, and the energy consumption required in the rectification process is reduced. The energy is saved by more than 45%, and the circulating water consumption is reduced by more than 28%. Effectively solves the problem of separation of butylene and butane, the purity of isobutane is more than or equal to 99.8 percent, and the yield is more than or equal to 95 percent.
Description
Technical Field
The invention relates to a butane refining method, in particular to an energy-saving process method for recovering butane in mixed C4.
Background
With the increase of ethylene production and crude oil processing capacity in China, a steam cracking device and a catalytic cracking device are rich in a large amount of C4, and the high alkane content in the mixed C4 restricts the effective utilization of olefin. The main components of the mixed C4 are butylene and butane, which have close boiling points and are difficult to separate by ordinary rectification.
Patent CN103508830A proposes a method for separating alkane and alkene in etherified C4 fraction, in the method, firstly, etherified C4 fraction reacts with acetic acid to produce sec-butyl acetate, and then the sec-butyl acetate is cracked to obtain acetic acid and n-butene. However, after etherification, more than one olefin in C4 can be reacted with other olefins to form other impurities. The method is high in cost and high in additional value of sec-butyl acetate, and resource waste is caused by separation of alkane and olefin in a cracking mode of synthesizing sec-butyl acetate.
Patent CN106478337A proposes a separation method of C4 olefin/alkane, which adopts high-selectivity adsorbent to prepare isobutene and 1-butene with purity of 99 wt% -99.5 wt% by an adsorption-rectification coupling process. However, the adsorption-rectification coupling process is adopted, so that the process is complex and the cost is high.
Patent CN1358697A proposes a method for separating butane and butene by using methyl ethyl ketone series mixed solvent. The method adopts the mixture of methyl ethyl ketone and polar solvent such as N-formyl morpholine, sulfolane, N-methyl pyrrolidone and the like as the solvent, and the butane and the butene are separated by extractive distillation with the solvent ratio of 9-15. The method for separating butane and butene by adopting extractive distillation is an effective process method, however, the extraction ratio required for achieving the higher separation purpose is generally more than or equal to 15 by adopting the extractive distillation process method, so that the theoretical plate number is higher, the requirements on equipment cost are higher, and the energy consumption is higher.
The invention provides an energy-saving process method for recovering butane in mixed C4, which takes mixed C4 as a raw material, not only can realize the separation of olefin and alkane through heat integration, but also fully utilizes the heat with different tastes in the butane recovery process, greatly reduces the energy consumption required in the rectification process through process optimization, reduces the energy consumption by more than 45 percent compared with the energy consumption of the traditional process, reduces the condensed water consumption by more than 28 percent, has simple flow and easy realization, and greatly improves the economic benefit and the social benefit of enterprises.
Disclosure of Invention
The invention provides an energy-saving process method for recovering butane in mixed C4, which takes mixed C4 as a raw material, not only can realize the separation of olefin and alkane through heat integration, but also fully utilizes the heat with different tastes in the butane recovery process, greatly reduces the energy consumption required in the rectification process through process optimization, reduces the energy consumption by more than 45 percent compared with the energy consumption of the traditional process, reduces the condensed water consumption by more than 28 percent, has simple distillation process, is easy to realize, and greatly improves the economic benefit and social benefit of enterprises.
The invention is realized by adopting the following technical scheme:
an energy-saving process method for recovering butane in mixed C4 comprises an alkane crude separation tower, an extraction rectification upper tower, an extractant recovery I tower, an extractant recovery II tower and a rectification device consisting of a heat exchanger, and is characterized in that gas phase at the top of a T101 tower of the alkane crude separation tower is condensed and cooled by a condenser E103 at the top of the alkane crude separation tower and then enters the lower part of a T102 extraction rectification tower, part of materials at the bottom of the tower are heated and gasified by a reboiler E102 of the alkane crude separation tower and then return to the bottom of the T101 tower, and part of the materials are heated and gasified by a heat exchanger E101 of the alkane crude separation tower and then return to the bottom of the T101 tower, and the other parts of the materials are extracted as products; a circulating extractant is added from the upper part of an extraction rectifying tower T102, gas phase at the top of the extraction rectifying tower T102 is extracted and enters the bottom of an upper tower T103 of the extraction rectifying tower, the side line extracted material of the extraction rectifying tower T102 is heated and gasified by an intermediate heat exchanger E201 of the extraction rectifying tower and then returns to the lower part of the extraction rectifying tower T102, part of the tower bottom material is heated and gasified by an extraction rectifying tower reboiler E202 and then returns to the tower bottom of the extraction rectifying tower T102, and part of the tower bottom material serving as a raw material enters an extractant recovery I tower T104; isobutane products are extracted from the top of the upper tower T103 of the extraction and rectification tower, part of the tower bottom materials are heated and gasified by an upper tower reboiler E301 of the extraction and rectification tower and then return to the tower bottom of the upper tower T103 of the extraction and rectification tower, and part of the tower bottom materials are returned to the extraction and rectification tower T102 as reflux materials; olefin is extracted from the top of the extractant recovery tower I T104, part of the tower kettle returns to the bottom of the extractant recovery tower I T104 after being heated and gasified by an extractant recovery tower I reboiler E401, and part of the olefin enters an extractant recovery tower II T105 as a raw material; the gas phase at the top of the extraction agent recovery II tower T105 enters an upper tower reboiler E301 of an extraction rectification tower for heat exchange, a part of the gas phase is condensed and cooled by an extraction agent recovery II tower condenser E502 and returns to the top of the extraction agent recovery II tower T105 as reflux, a part of the gas phase enters an extraction agent recovery I tower T104 as a raw material, a part of the material at the bottom of the extraction agent recovery II tower T105 is heated and gasified by an extraction agent recovery II tower reboiler E501 and returns to the bottom of the extraction agent recovery II tower T105, a part of the material enters an intermediate heat exchanger E201 of the extraction rectification tower for heat exchange and then enters an alkane crude fractionating tower heat exchanger E101 for heat exchange, and then the material returns to the extraction rectification tower T102 as a circulating.
The invention is characterized in that:
1. the raw material is pretreated by an alkane and alkene crude separation tower T101, and alkane and alkene are roughly separated by rectification, so that the dosage of an extracting agent required by an extraction and rectification tower can be greatly reduced, the extraction ratio is reduced, and the energy consumption is further reduced under the condition of not influencing the product yield; the heat exchanger E101 is adopted in the tower bottom of the T101 to exchange heat between the tower bottom material and the high-grade heat of the extractant at the tower bottom of the extractant recovery II tower T105, so that the energy consumption is further saved, and the consumption of circulating water is reduced;
2. an intermediate reboiler E201 of the extraction rectifying tower T102 is added, the boiling point of alkane at the upper part of the extraction rectifying tower is lower, so that the intermediate reboiler can be added at a proper position, and the extractant is used for recovering high-grade heat of the extractant at the bottom of the tower T105 of the tower II, so that the energy can be saved, and the consumption of circulating water can be reduced;
3. the upper extractive distillation tower T103 is added, and the material of the upper extractive distillation tower is mainly isobutane, so the heat required by a reboiler E301 is low in taste, and the requirement of heating by the heat of steam at the top of the T105 tower of the II tower recovered by an extractant can be met, so that the energy consumption can be saved, and the consumption of T105 condensation cooling circulating water can be reduced.
The column apparatus of the present invention may be either a packed column or a tray column.
The process conditions of the invention are as follows: the operation pressure of the alkane and alkene crude separation tower T101 is 0.5-1.2MPa, the operation pressure of the extraction and rectification tower T102 is 0.5-1.2MPa, the operation pressure of the extraction and rectification upper tower T103 is 0.5-1.2MPa, the operation pressure of the extraction agent recovery tower I T104 is 0.5-1.2MPa, and the operation pressure of the extraction agent recovery tower II T105 is 0.1-0.6 MPa.
The extracting agent adopted by the invention is one or a mixed solvent of methyl ethyl ketone, morpholine and N-methyl pyrrolidone in any proportion.
The mass ratio (extraction ratio) of the extracting agent to the C4 is 4-10.
The purity of the refined isobutane is more than or equal to 99.8 percent, and the yield is more than or equal to 95 percent.
The invention provides an energy-saving method for recovering butane in mixed C4, which takes mixed C4 as a raw material, not only can realize the separation of olefin and alkane through heat integration, but also fully utilizes the heat of different grades in the butane recovery process, and greatly reduces the energy consumption required in the rectification process through process optimization. The beneficial results of the invention are:
a) by optimizing the process and heat integration, the energy can be saved by more than 45%, and the circulating water consumption is reduced by more than 28%.
b) Effectively solving the problem of separation of the butylene and the butane, and obtaining the isobutane with the purity of more than or equal to 99.8 percent and the yield of more than or equal to 95 percent
Drawings
FIG. 1: a schematic of an energy saving device to recover butane in blend C4;
a T101 alkane and alkene crude separation tower, a T102 extractive distillation tower, a T103 extractive distillation upper tower, a T104 extractant recovery tower I and a T105 extractant recovery tower II; the system comprises an E101 alkane and alkene crude separation tower kettle heat exchanger, an E102 alkane and alkene crude separation tower reboiler, an E103 alkane and alkene crude separation tower top condenser, an E201 extractive distillation tower middle heat exchanger, an E202 extractive distillation tower reboiler, an E301 extractive distillation tower top reboiler, an E302 extractive distillation tower top condenser, an E401 extractant recovery tower I reboiler, an E402 extractant recovery tower I top condenser, an E501 extractant recovery tower II reboiler and an E502 extractant recovery tower II top condenser.
Detailed Description
The invention provides an energy-saving process for recovering butane in mixed C4, which takes mixed C4 as a raw material, not only can realize the separation of olefin and alkane through heat integration, but also fully utilizes the heat with different tastes in the butane recovery process, and greatly reduces the energy consumption required in the rectification process through process optimization. The following further describes the method of implementation with reference to the application examples.
Example 1
The present invention will be further described with reference to fig. 1 and the following detailed description.
The raw materials comprise:
| isobutane | N-butane | N-butene | Butene of trans-butene | N-pentane | Isobutene | Cis-butenediol | 1, 3-butadiene |
| 0.4800 | 0.1600 | 0.1300 | 0.1230 | 0.0060 | 0.0020 | 0.0980 | 0.0010 |
An energy-saving process method for recovering butane in mixed C4 comprises an alkane and alkene rough separation tower, an extraction rectification tower, an upper extraction rectification tower, an extractant recovery tower I, an extractant recovery tower II and a rectification device consisting of a heat exchanger, and is characterized in that gas phase at the top of a T101 tower of the alkane and alkene rough separation tower is condensed and cooled by a tower top condenser E103 and then enters the lower part of a T102 extraction rectification tower, part of materials at a tower bottom are heated and gasified by a reboiler E102 and then return to the tower bottom of the T101 tower, and part of the materials are heated and gasified by the heat exchanger E101 and then return to the tower bottom of the T101 tower, and the other part of the materials are; a circulating extractant is added from the upper part of an extraction rectifying tower T102, gas phase extracted from the top of the T102 tower enters the bottom of an upper tower T103 of the extraction rectifying tower, materials extracted from the side line of the T102 tower are heated and gasified by an intermediate heat exchanger E201 and then return to the lower part of the T102 tower, a part of materials in a tower bottom are heated and gasified by a reboiler E202 and then return to the tower bottom of the T102 tower, and a part of materials as a raw material enter a tower T104 of an extractant recovery I; isobutane products are extracted from the top of the upper tower T103 of the extraction and rectification tower, part of the tower bottom materials are heated and gasified by a reboiler E301 and then return to the tower bottom of the T103, and part of the tower bottom materials are returned to the extraction and rectification tower T102 as reflux materials; olefin is extracted from the top of the T104 tower of the extractant recovery I tower, part of the tower kettle returns to the T104 tower kettle after being heated and gasified by a reboiler E401, and part of the tower kettle is used as a raw material to enter the extractant recovery II tower T105; and after the gas phase at the top of the T105 tower enters a reboiler E301 of a T103 tower kettle for heat exchange, a part of the gas phase is condensed and cooled by a condenser E502 and returns to the top of the T105 tower as reflux, a part of the gas phase enters T104 as a raw material, a part of the material at the bottom of the T105 tower returns to the T105 tower kettle after being heated and gasified by a reboiler E501, a part of the material enters E201 for heat exchange and then enters E101 for continuous heat exchange, and then the material returns to T102 as a circulating.
The operating pressure of each column was as follows:
the operation pressure of the extraction and rectification tower T101 is 0.7MPa, the operation pressure of the extraction and rectification tower T102 is 0.75MPa, the operation pressure of the extraction and rectification upper tower T103 is 0.75MPa, the operation pressure of the extractant recovery tower I T104 is 0.65MPa, and the operation pressure of the extractant recovery tower II T105 is 0.35 MPa.
The purity of refined isobutane was 99.8%, and the yield was 95%.
Energy-saving and water-saving effects (feeding amount 1000 kg/h):
| condenser kcal/h | Reboiler kcal/h | |
| Conventional process | -838810 | 530543 |
| Heat integration process | -599761 | 291493 |
| Energy-saving% | 28.5 | 45.1 |
Example 2
The raw materials comprise:
| isobutane | N-butane | N-butene | Butene of trans-butene | N-pentane | Isobutene | Cis-butenediol | 1, 3-butadiene |
| 0.4800 | 0.1600 | 0.1300 | 0.1230 | 0.0060 | 0.0020 | 0.0980 | 0.0010 |
The energy saving process for recovering butane from blend C4 of this example is the same as example 1.
The operating pressure of each column was as follows:
the operation pressure of the extraction and rectification tower T101 is 0.5MPa, the operation pressure of the extraction and rectification tower T102 is 0.5MPa, the operation pressure of the extraction and rectification upper tower T103 is 0.5MPa, the operation pressure of the extraction agent recovery tower I T104 is 0.5MPa, and the operation pressure of the extraction agent recovery tower II T105 is 0.1 MPa.
The purity of refined isobutane was 99.8%, and the yield was 95%.
Energy-saving and water-saving effects (feeding amount 1000 kg/h):
| condenser kcal/h | Reboiler kcal/h | |
| Conventional process | -791018 | 431354 |
| Heat integration process | -550691 | 247735 |
| Energy-saving% | 30.0 | 42.6 |
Example 3
The raw materials comprise:
| isobutane | N-butane | N-butene | Butene of trans-butene | N-pentane | Isobutene | Cis-butenediol | 1, 3-butadiene |
| 0.4800 | 0.1600 | 0.1300 | 0.1230 | 0.0060 | 0.0020 | 0.0980 | 0.0010 |
The energy saving process for recovering butane from blend C4 of this example is the same as example 1.
The operating pressure of each column was as follows:
the operating pressure of the extraction and rectification tower T101 is 1.2MPa, the operating pressure of the extraction and rectification tower T102 is 1.2MPa, the operating pressure of the extraction and rectification upper tower T103 is 1.2MPa, the operating pressure of the extractant recovery tower I T104 is 1.2MPa, and the operating pressure of the extractant recovery tower II T105 is 0.6 MPa.
The purity of refined isobutane was 99.8%, and the yield was 95%.
Energy-saving and water-saving effects (feeding amount 1000 kg/h):
| condenser kcal/h | Reboiler kcal/h | |
| Conventional process | -1006572 | 636651 |
| Heat integration process | -779689 | 378941 |
| Energy-saving% | 22.5 | 40.5 |
Although the method and the preparation technique of the present invention have been described by way of preferred embodiments, it is obvious to those skilled in the art that the method and the technical route described herein can be modified or recombined to realize the final preparation technique without departing from the content, spirit and scope of the present invention. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and content of the invention.
Claims (8)
1. An energy-saving process method for recovering butane in mixed C4 comprises an alkane crude separation tower, an extraction rectification upper tower, an extractant recovery I tower, an extractant recovery II tower and a rectification device consisting of a heat exchanger, and is characterized in that gas phase at the top of a T101 tower of the alkane crude separation tower is condensed and cooled by a condenser E103 at the top of the alkane crude separation tower and then enters the lower part of a T102 extraction rectification tower, part of materials at the bottom of the tower are heated and gasified by a reboiler E102 of the alkane crude separation tower and then return to the bottom of the T101 tower, and part of the materials are heated and gasified by a heat exchanger E101 of the alkane crude separation tower and then return to the bottom of the T101 tower, and the other parts of the materials are extracted as products; a circulating extractant is added from the upper part of an extraction rectifying tower T102, gas phase at the top of the extraction rectifying tower T102 is extracted and enters the bottom of an upper tower T103 of the extraction rectifying tower, the side line extracted material of the extraction rectifying tower T102 is heated and gasified by an intermediate heat exchanger E201 of the extraction rectifying tower and then returns to the lower part of the extraction rectifying tower T102, part of the tower bottom material is heated and gasified by an extraction rectifying tower reboiler E202 and then returns to the tower bottom of the extraction rectifying tower T102, and part of the tower bottom material serving as a raw material enters an extractant recovery I tower T104; isobutane products are extracted from the top of the upper tower T103 of the extraction and rectification tower, part of the tower bottom materials are heated and gasified by an upper tower reboiler E301 of the extraction and rectification tower and then return to the tower bottom of the upper tower T103 of the extraction and rectification tower, and part of the tower bottom materials are returned to the extraction and rectification tower T102 as reflux materials; olefin is extracted from the top of the extractant recovery tower I T104, part of the tower kettle returns to the bottom of the extractant recovery tower I T104 after being heated and gasified by an extractant recovery tower I reboiler E401, and part of the olefin enters an extractant recovery tower II T105 as a raw material; the gas phase at the top of the extraction agent recovery II tower T105 enters an upper tower reboiler E301 of an extraction rectification tower for heat exchange, a part of the gas phase is condensed and cooled by an extraction agent recovery II tower condenser E502 and returns to the top of the extraction agent recovery II tower T105 as reflux, a part of the gas phase enters an extraction agent recovery I tower T104 as a raw material, a part of the material at the bottom of the extraction agent recovery II tower T105 is heated and gasified by an extraction agent recovery II tower reboiler E501 and returns to the bottom of the extraction agent recovery II tower T105, a part of the material enters an intermediate heat exchanger E201 of the extraction rectification tower for heat exchange and then enters an alkane crude fractionating tower heat exchanger E101 for heat exchange, and then the material returns to the extraction rectification tower T102 as a circulating.
2. The process as claimed in claim 1, wherein the raw material is first pretreated by an alkane and alkene crude separation column T101, and the bottom of T101 is subjected to heat exchange with the high-temperature extractant extracted from the bottom of an extractant recovery column IIT 105 by using a heat exchanger E101.
3. The method as set forth in claim 1, characterized in that the extractive distillation column T102 exchanges heat with the high-temperature extractant taken from the bottom of the extractant recovery column IIT 105 by using an intermediate reboiler E201.
4. The method as set forth in claim 1, characterized in that an extractive distillation upper column T103 is added, and a column bottom reboiler E301 of the extractive distillation upper column T103 is heated by extracting a gas phase from a column top of the extractive distillation II.
5. The method as claimed in claim 1, wherein the operation pressure of the crude separation column T101 for the alkane and the alkene is 0.5-1.2MPa, the operation pressure of the extractive distillation column T102 is 0.5-1.2MPa, the operation pressure of the upper column T103 for the extractive distillation is 0.5-1.2MPa, and the operation pressure of the extraction agent recovery column I T104 is 0.5-1.2 MPa.
6. The process as claimed in claim 1, wherein the extractant recovery II column T105 is operated at a pressure of from 0.1 to 0.6 MPa.
7. The process as claimed in claim 1, characterized in that the column apparatus is a packed column or a tray column.
8. The method as claimed in claim 1, wherein the extractant is one or a mixture of methyl ethyl ketone, morpholine and N-methyl pyrrolidone in any proportion, and the mass ratio of the extractant to C4 is 4-10.
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