CN1131189C - Cracking gas compressing process in ethylene production - Google Patents
Cracking gas compressing process in ethylene production Download PDFInfo
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- CN1131189C CN1131189C CN01118358A CN01118358A CN1131189C CN 1131189 C CN1131189 C CN 1131189C CN 01118358 A CN01118358 A CN 01118358A CN 01118358 A CN01118358 A CN 01118358A CN 1131189 C CN1131189 C CN 1131189C
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The present invention belongs to the technical field of chemical industry. The present invention comprises five compression working sections, wherein a first compression working section and a second compression working section are respectively composed of a compressor and a direct cooling tower, a third compression working section, a fourth compression working section and a fifth compression working section are respectively composed of a compressor, a gas-liquid separating tank and an indirect condenser, and the temperature of an inlet of the compressor is controlled between 20 DEG C and 25 DEG C. The present invention can improve the processing capacity of compression systems under the condition of original compressors, and has the advantages of energy saving, lowered consumption, reduced investment and lowered production cost of ethylene.
Description
The invention belongs to chemical technology field, particularly a kind of ethylene production splitting gas compression novel process.
The splitting gas compression process generally is made up of five workshop sections in the current domestic ethylene production, and each workshop section is made up of compressor, vapor-liquid separation tank and indirect condenser substantially.Its processing step is: after gas enters the compressed machine compression of first workshop section, part heavy constituent condensation is separated out in vapor-liquid separation tank, remove gas after the part heavy constituent and reach 38 C enter next workshop section's compressor again after heat exchange, the process of cooling pressure-losses is about 250kPa.The part light constituent of separating out in the vapor-liquid separation tank in the lime set enters next workshop section's compressor equally behind the water vapour stripping.Other workshop sections similarly.
Because vapor-liquid separation tank has only been finished the once balance phase-splitting in the above-mentioned flow process, separation efficiency is low, also contains a large amount of heavy components in the gas phase, also remains a large amount of light constituents in the lime set simultaneously, needs the consume water steam to carry out gas in gas stripping column and carries.
Corresponding when expanding production with the ethylene producing device of above-mentioned compression process, owing to the removal efficiency of compression process heavy constituent is lower, with expand production before compare, compression load almost is linear growth with treatment capacity, often needs to purchase the bigger compressor of new draught.This compressor expense is invested very greatly about about 2,000 ten thousand yuan-3,000 ten thousand yuan, and the production cost of ethene is increased.
The objective of the invention is for overcoming the weak point of prior art, propose a kind of splitting gas compression new process of ethylene production, make its processing power that under the condition of existing compressor, improves compression system, energy-saving and cost-reducing, reduce investment, reduce the production cost of ethene.
Cracking gas compressing process in a kind of ethylene production that the present invention proposes; Comprise five workshop sections, it is characterized in that: one section and two sections are made of compressor and direct cooling tower; Three sections, four sections and five sections are formed by compressor, vapor-liquid separation tank and indirect condenser, intersegmentally add a counter current contact rectifying tower at two sections and three;
Specifically may further comprise the steps:
(1) after gas enters the compressed machine P1 of first workshop section compression,, part heavy constituent condensation is separated out, remove gas after the part heavy constituent and after heat exchange, reach 20 ℃-25 ℃ and enter the second compressor P2 of workshop section again through directly cooling tower T1 cooling;
(2) second workshop section's compressor P2 exit gass enter counter current contact rectifying tower T2, isolate the part heavy component in the splitting gas at the bottom of the tower, and overhead gas temperature after heat exchange is reduced to 20 ℃-25 ℃ and entered the 3rd compressor P3 of workshop section again;
(3) after gas entered the compressed machine compression of the 3rd workshop section, part heavy constituent condensation was separated out in vapor-liquid separation tank, removed gas after the part heavy constituent and reached 20 ℃-25 ℃ enter down the 4th workshop section's compressor again after heat exchange.The 4th is identical with third step with the 5th intersegmental flow process.
Characteristics of the present invention are:
Because one section and two intersegmental condensers and separating tanks are directly cooled tower T1 replacement, directly cooling tower has the effect of water cooler, make the once balance of two sections original suction tanks change the repeatedly balance of splitting gas and water counter current contact into simultaneously, not only heat-transfer effect is good, and has an effect of mass transmitting, cat head heavy component content is reduced, and the splitting gas volume reduces.On the other hand, the splitting gas temperature out is reduced to 20 ℃-25 ℃ by 38 ℃ of former technology, and volume is decreased, thereby has alleviated the burdens of two sections compression P2.Adopt direct cooling tower also can make pressure drop drop to 20kPa, can make the inlet pressure of two sections compressor P2 improve about 14% like this by the 250kPa of former technology.Calculating shows: utilize water coolant directly to cool off, can save a large amount of energy consumptions.Because reducing of pressure drop, the reduction of energy consumption makes two sections compression ratios bring up to 1.9 by 2.5, can save the power about 6～10% of compressor.Because the splitting gas temperature out drops to 20 ℃ by original 38 ℃, can make the splitting gas volume reduce 6～8%.Heavy component also makes the load of next stage compressor reduce about 3% in the minimizing of water wash column outlet simultaneously.After taking above measure, the compressor processing power can improve 15～20%.
Two sections and the three intersegmental counter current contact rectifying tower T2 that adopted further isolate the heavy component in the splitting gas, have reduced by the load of three sections compressor P3.Owing to isolate heavy component in the splitting gas, can make cracking compressor processing power improve 2～3%.The splitting gas temperature that enters three sections compressions is simultaneously reduced to 20 ℃ equally, can alleviate the load about 6～8% of cracking gas compressor again.
Three sections with four intersegmental and four sections no longer change with five intersegmental flow processs, just control enters that temperature in is 20 ℃ (former flow process is 38 ℃) between compressor section, reduce to enter the heavy component content and the splitting gas volume of next stage compressor, save the load of next stage compressor.
Net effect of the present invention mainly shows as:
1. compressor load reduces by 20%, increases the compressor processing power more than 15%; 2. reduce the energy consumption 20～30% of compressor assembly.
The present invention can be widely used in the ethylene distillation.
Fig. 1 is an ethylene production cracking gas compressing process schematic flow sheet of the present invention.
Ethylene production cracking gas compressing process of the present invention is described in detail as follows by embodiment and accompanying drawing.
1, one section and two intersegmental condenser and separating tanks are replaced with direct cooling tower T1, the cooling tower theoretical stage is 4 grades, 18 ℃ of temperature of cooling water, and the ratio of cooling water amount and splitting gas consumption is 3: 1.Transform back splitting gas temperature out and reduce to 20 ℃ by 38 ℃ of former technology, owing to isolate heavy constituent in the splitting gas, the splitting gas volume reduces 9%, process of cooling generation pressure drop drops to 20kPa by the 250kPa of former technology, can make the inlet pressure of two sections compressor P2 improve 16% like this, make two sections compression ratios bring up to 1.9, save the power 8% of compressor by 2.5.
Two sections and the three intersegmental counter current contact rectifying tower T2 that adopted, theoretical stage is 10 grades, owing to isolate heavy component in the splitting gas, the compressor processing power improves 2%.The splitting gas temperature that enters three sections compressions is simultaneously reduced to 20 ℃ equally, can reduce the load 6% of cracking gas compressor again.
Three sections and four intersegmental and four sections and the controls of five intersegmental flow processs enter temperature between compressor section and reduce to 20 ℃ by 38 ℃ of former technology, can reduce to enter the heavy component content of next stage compressor, and the splitting gas volume reduces 2%.
2, one section and two intersegmental direct cooling tower T1 theoretical stages are 5 grades, 20 ℃ of temperature of cooling water, and the ratio of cooling water amount and splitting gas consumption is 5: 1.Transform back splitting gas temperature out and reduce to 20 ℃ by 38 ℃ of former technology, the splitting gas volume reduces 7%, and it is 25kPa that process of cooling produces pressure drop, and the inlet pressure of two sections compressors improves about 14%, two sections compression ratios bring up to 1.95 by 2.5, save the power 8% of compressor.
The theoretical stage of two sections and three intersegmental counter current contact rectifying tower T2 is 11 grades, and the compressor processing power improves 2.2%.The splitting gas temperature that enters three sections compressions is simultaneously reduced to 20 ℃ equally, can reduce the load 6% of cracking gas compressor.
Three sections and four intersegmental and four sections and the controls of five intersegmental flow processs enter temperature between compressor section and reduce to 20 ℃ by 38 ℃ of former technology, and the splitting gas volume reduces 2%.
3, one section and two intersegmental direct cooling tower T1 theoretical stages are 4 grades, 19 ℃ of temperature of cooling water, and the ratio of cooling water amount and splitting gas consumption is 4: 1.Transform back splitting gas temperature out and reduce to 20 ℃ by 38 ℃ of former technology, the splitting gas volume reduces 8%, and it is 26kPa that process of cooling produces pressure drop, and the inlet pressure of two sections compressors improves about 14%, two sections compression ratios bring up to 2 by 2.5, save the power 7.5% of compressor.
The theoretical stage of two sections and three intersegmental counter current contact rectifying tower T2 is 9 grades, and the compressor processing power improves 2%.The splitting gas temperature that enters three sections compressions is 22 ℃, and the load of cracking gas compressor reduces 5.5%.
Three sections and four intersegmental and four sections and the controls of five intersegmental flow processs enter temperature between compressor section and reduce to 20 ℃ by 38 ℃ of former technology, can reduce to enter the heavy component content of next stage compressor, and the splitting gas volume reduces 2.5%.
Claims (1)
1, the cracking gas compressing process in a kind of ethylene production; Comprise five workshop sections, it is characterized in that: one section and two sections are made of compressor and direct cooling tower; Three sections, four sections and five sections are formed by compressor, vapor-liquid separation tank and indirect condenser, intersegmentally add a counter current contact rectifying tower at two sections and three; Specifically may further comprise the steps:
(1) after gas enters the compressed machine P1 of first workshop section compression,, part heavy constituent condensation is separated out, remove gas after the part heavy constituent and after heat exchange, reach 20 ° ℃-25 ° ℃ and enter the second compressor P2 of workshop section again through directly cooling tower T1 cooling;
(2) second workshop section's compressor P2 exit gass enter counter current contact rectifying tower T2, isolate the part heavy component in the splitting gas at the bottom of the tower, and overhead gas temperature after heat exchange is reduced to 20 ℃-25 ℃ and entered the 3rd compressor P3 of workshop section again;
(3) after gas entered the compressed machine compression of the 3rd workshop section, part heavy constituent condensation was separated out in vapor-liquid separation tank, removed gas after the part heavy constituent and reached 20 ℃-25 ℃ enter down the 4th workshop section's compressor again after heat exchange; The 4th is identical with third step with the 5th intersegmental flow process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN01118358A CN1131189C (en) | 2001-05-25 | 2001-05-25 | Cracking gas compressing process in ethylene production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN01118358A CN1131189C (en) | 2001-05-25 | 2001-05-25 | Cracking gas compressing process in ethylene production |
Publications (2)
| Publication Number | Publication Date |
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| CN1323768A CN1323768A (en) | 2001-11-28 |
| CN1131189C true CN1131189C (en) | 2003-12-17 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN01118358A Expired - Fee Related CN1131189C (en) | 2001-05-25 | 2001-05-25 | Cracking gas compressing process in ethylene production |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100538074C (en) * | 2007-07-30 | 2009-09-09 | 四川美丰化工股份有限公司 | Optimize the method for M type compressor operation |
| CN101358143B (en) * | 2008-08-28 | 2012-08-15 | 天津大学 | Ethylene quenching apparatus and compressing energy-saving technique |
| CN103423969A (en) * | 2013-08-30 | 2013-12-04 | 北京麦科直通石化工程设计有限公司 | Method for optimizing ethylene device compression area and reducing outlet pressure of cracking furnace |
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- 2001-05-25 CN CN01118358A patent/CN1131189C/en not_active Expired - Fee Related
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| CN1323768A (en) | 2001-11-28 |
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