CN101332408A - Preparation method of DHA jellyfish egg polypeptides freeze-dry powder - Google Patents
Preparation method of DHA jellyfish egg polypeptides freeze-dry powder Download PDFInfo
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- CN101332408A CN101332408A CNA2008100220542A CN200810022054A CN101332408A CN 101332408 A CN101332408 A CN 101332408A CN A2008100220542 A CNA2008100220542 A CN A2008100220542A CN 200810022054 A CN200810022054 A CN 200810022054A CN 101332408 A CN101332408 A CN 101332408A
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Abstract
The invention relates to a recovery device for the mixed exhaust gas of chlorine hydride and sulfur dioxide in the protogen production, and belongs to the technical field of the exhaust gas recovery device in the production of medical and chemical-industrial products. The recovery device comprises at least more than one group of water absorption mechanism and a reaction mechanism, wherein, each water absorption mechanism comprises an absorption tower, a storage tank and a circulation pump, wherein, the storage tank is positioned below the absorption tower, a gas introduction interface of the storage tank is connected with a gas eduction interface at the bottom part of the absorption tower by a first pipeline, an exhaust gas introduction pipeline is connected on a gas introduction interface at the top of the absorption tower, a gas eduction port of the storage tank is connected with one end of a second pipeline, the other end of the second pipeline is connected with an adjacent group of water absorption mechanism and the circulation pump is connected between the water absorption tower and the storage tower by a third pipeline and a fourth pipeline; the reaction mechanism comprises a reaction kettle and a vacuum pump, wherein, a feed inlet of the reaction kettle is connected with the second pipeline of the last group of water absorption mechanism and the vacuum pump is connected with the reaction kettle by a fifth pipeline. The recovery device has the advantages of being beneficial to protecting the environment and the resources as well as reducing the production cost.
Description
Technical field
The invention belongs to the waste gas recovering device technical field in the medication chemistry production, be specifically related to a kind of lipoic acid produce in the retracting device of hydrogen chloride and sulfur dioxide mix waste gas.
Background technology
As is known in the industry, the acidylate liquid in lipoic acid intermediate reducing solution and the chloride process need adopt thionyl chloride to carry out chlorination reaction, can produce hydrogen chloride and sulfur dioxide mix waste gas in chlorination reaction process.In the prior art, normally with hydrogen chloride and sulfur dioxide mix waste gas directly to external world's discharging, thereby produce following technical problem: at first, hydrogen chloride and sulfur dioxide mix waste gas directly arranged to the external world can cause pollution environment; Secondly, can cause the unreasonable waste of resource, because hydrogen chloride and sodium sulfite are widely used in the production of chemical products, and sodium sulfite consumes the environment-friendly products of sulfur dioxide and has more and have broad application prospects as a kind of; Also have, hydrogen chloride and sulfur dioxide are not added the increase that recovery can cause the production cost of lipoic acid manufacturing enterprise self, the raw material because hydrogen chloride is absolutely necessary in the production of lipoic acid for example, need use hydrogen chloride to the acidification reaction of digest of ethereal lipoate.Therefore,, have positive meaning so undoubtedly, that is: help protecting environment if the mix waste gas of hydrogen chloride in the lipoic acid production and sulfur dioxide can be reclaimed; Help to economize on resources; Be of value to the production cost that reduces enterprise self.The technical scheme that the present invention will introduce below is based on producing under this background.
Summary of the invention
Task of the present invention be to provide a kind of useful to environmental protection, favourable and lipoic acid that can reduce the production cost of enterprise in the utilization of resources in producing hydrogen chloride and the retracting device of sulfur dioxide mix waste gas.
Task of the present invention is finished like this, the hydrogen chloride during a kind of lipoic acid is produced and the retracting device of sulfur dioxide mix waste gas, it comprises at least one group of above and water absorbing mechanism and reaction mechanism that be one another in series and connect, each water absorbing mechanism comprises the absorption tower, storage tank and circulating pump, storage tank is positioned at the below on absorption tower, the gas of storage tank is introduced interface and is drawn the interface connection by the gas of first pipeline and bottom, absorption tower, the gas at the top on absorption tower is introduced and is connect the waste gas introduction pipeline on the interface, the gas outlet of storage tank and a client link of second pipeline, the other end of second pipeline and one group of adjacent water absorbing mechanism connection, circulating pump is by the 3rd, the 4th pipeline connect in series is between suction tower and storage tank; Described reaction mechanism comprises reactor and vavuum pump, and the charging aperture of reactor is connect by the 5th pipeline and reactor with last not second pipeline connection of one group of water absorbing mechanism, vavuum pump.
In a specific embodiment of the present invention, described absorption tower is a waste gas absorption tower.
In another specific embodiment of the present invention, the reactor that described reactor stirs for band.
In also specific embodiment of the present invention, the quantity of described water absorbing mechanism is 2～5 groups.
In another specific embodiment of the present invention, the quantity of described water absorbing mechanism is 2～4 groups.
In another specific embodiment of the present invention, the quantity of described water absorbing mechanism is 3 groups, wherein, the 4th pipeline of second group of water absorbing mechanism is provided with first valve, and the 4th pipeline of second group of water absorbing mechanism connects mutually by the storage tank of the 6th pipeline with first group of water absorbing mechanism; The 4th pipeline of the 3rd group of water absorbing mechanism is provided with second valve, and the 4th pipeline of the 3rd group of water absorbing mechanism connects mutually by the storage tank of the 7th pipeline with second group of water absorbing mechanism.
More of the present invention and in specific embodiment, the vacuum of described vavuum pump is-0.08～0.1MPa.
In of the present invention and then specific embodiment, the vacuum of described vavuum pump is-0.09MPa.
In the water of technical scheme provided by the present invention owing to the storage tank that hydrogen chloride gas can be dissolved in water absorbing mechanism; and the reactor that sulfur dioxide gas can be introduced reaction mechanism is used to prepare seven water sodium sulfites; therefore not only help protecting environment and economize on resources; and can also reduce the production cost of enterprise; because the hydrogen chloride solution that reclaims can be used in the lipoic acid production, and sulfur dioxide can be to market sale after preparing seven water sodium sulfites.
Description of drawings
Accompanying drawing is a specific embodiment schematic diagram of the present invention.
The specific embodiment
Ask for an interview accompanying drawing, as a preferred embodiment, provided three groups of identical water absorbing mechanisms 1 consistent with action principle of structure, the applicant is being that one group of water absorbing mechanism 1 on the left side is that example is described in detail by first group shown in the drawings at present.Comprise the absorption tower 11, storage tank 12 and the circulating pump 13 that are used to absorb waste gas, absorption tower 11 can be bearing on the terrace 3 by the support (not shown), the position of storage tank 12 should remain below the degree of the height on absorption tower 11, that is to say that storage tank 12 is positioned at the below on absorption tower 11, the top of storage tank 12 is equipped with atmospheric valve 123.It is XDT101 type polypropylene tail gas absorber that the model by the production and sales of Taicang, the Jiangsu Province, China rotten sterilization of new joint defence Engineering Co., Ltd is adopted on preferred but not absorption tower 11 that be limited to.The gas at 11 tops, absorption tower is introduced and is connected waste gas introduction pipeline 1121 on the interface 112, by this waste gas introduction pipeline 1121 hydrogen chloride and the sulfur dioxide mix waste gas that produces in for example chlorination reaction process in the lipoic acid production process is incorporated in the absorption tower 11.The gas of 11 bottoms, absorption tower is drawn interface 111 and is introduced interface 121 connections by first pipeline 1211 and the gas at storage tank 12 tops that fill water, after hydrogen chloride and sulfur dioxide mix waste gas are incorporated in the storage tank 12 by first pipeline 1211, sulfur dioxide is water insoluble because hydrogen chloride gas is soluble in water, therefore hydrogen chloride gas just separates with sulfur dioxide gas in storage tank 12, add the effect of circulating pump 13, hydrogen chloride gas can be dissolved in the storage tank 12 ideally.See by accompanying drawing, a client link of the inlet of circulating pump 13 and the 3rd pipeline 131, and the other end of the 3rd pipeline 131 and storage tank 12 connect; One client link of the liquid outlet of circulating pump 13 and the 4th pipeline 132, and the top on the other end of the 4th pipeline 132 and absorption tower 11 connects.
Because the water absorbing mechanism 1 that present embodiment is recommended has three groups, therefore, the gas at the top of the storage tank 12 of first group of water absorbing mechanism 1 by being connected second pipeline 1221 on the gas outlet 122 and second group of absorption tower 11 that is the one group of water absorbing mechanism 1 in centre shown in the drawings is introduced interface 112 and is connect.In like manner, the storage tank 12 of second group of water absorbing mechanism 1 is that the gas at top on absorption tower 11 of one group of water absorbing mechanism 1 on illustrated the right is introduced interface 112 and connect by second pipeline 1221 and the 3rd group, thereby constituting three grades of circulations absorbs, effectively hydrogen chloride is separated with the sulfur dioxide mix waste gas, make hydrogen chloride gas be tending towards absorbing totally.When the concentration of the hydrogen chloride solution in the storage tank 12 when sample analysis reaches blowing concentration, then emit reuse.Here alleged blowing concentration determines as required that usually the blowing concentration that the applicant selects is 〉=30%, and promptly the content of hydrogen chloride in water is 〉=30%.Before blowing, close first valve 4 on the 4th pipeline 132 of the circulating pump 13 that is located at second group of water absorbing mechanism 1 and close second valve 6 on the 4th pipeline 132 of the circulating pump 13 that is located at the 3rd group of water absorbing mechanism 1, open the 3rd valve 51 and the 4th valve of opening on the 7th pipeline 7 71 on the 6th pipeline 5, under the work of the circulating pump separately 13 of three groups of water absorbing mechanisms 1, making hydrogen chloride solution in the storage tank 12 of second group and the 3rd group water absorbing mechanism 1 be transferred to first group is in the storage tank 12 on the attached illustrated left side, specifically to be by the 6th, the 7th pipeline 5,7 take on.Owing to there are three storage tanks 12, therefore, when a storage tank 12 is not the 12 benefit entry of the storage tank in the right shown in the drawings to the end, the atmospheric valve on each storage tank 12 123 should be opened, after moisturizing finishes, promptly close atmospheric valve 123.
Because hydrogen chloride gas is absorbed by water absorbing mechanism 1, therefore by the end not second pipeline 1221 of one group of water absorbing mechanism 1 gas that is incorporated into reaction mechanism 2 be sulfur dioxide gas, sulfur dioxide gas enters (suction) reactor 21 under the effect of vavuum pump 22, be 32% sodium hydroxide solution as long as add concentration in the reactor 21 that has stirring this moment, and 50 ℃ of control reaction temperatures, when the pH of the reactant liquor in the reactor 21 value reaches 5.6, reactant liquor is switched to continuation absorption sulfur dioxide gas in another reactor (not shown), specifically be to add 32% sodium hydroxide solution again, when the pH of reactant liquor value reaches 9.5～10, then obtain sodium sulfite solution, cool off with brine ice, when temperature reaches 30 ℃, can separate out the crystalline solid of seven aqueous sodium persulfates in a large number, when temperature is reduced to 20 ℃, the material in the reactor be emitted, separate through centrifuge, obtain product seven water sodium sulfites.The vacuum of aforesaid vavuum pump 22 is-0.09MPa.Vavuum pump 22 is connect by the 5th pipeline 221 and reactor 21.
Claims (8)
1, the hydrogen chloride during a kind of lipoic acid is produced and the retracting device of sulfur dioxide mix waste gas, it is characterized in that it comprises at least one group of above and water absorbing mechanism (1) and reaction mechanism (2) that be one another in series and connect, each water absorbing mechanism (1) comprises absorption tower (11), storage tank (12) and circulating pump (13), storage tank (12) is positioned at the below of absorption tower (11), the gas of storage tank (11) is introduced interface (121) and is drawn interface (111) connection by first pipeline (1211) and the gas of bottom, absorption tower (11), the gas at the top on absorption tower (11) is introduced interface (112) and is gone up connection waste gas introduction pipeline (1121), the gas outlet (122) of storage tank (12) and a client link of second pipeline (1221), the other end of second pipeline (1221) and adjacent one group of water absorbing mechanism (1) connection, circulating pump (13) is by the 3rd, the 4th pipeline (131,132) connect in series is between suction tower (11) and storage tank (12); Described reaction mechanism (2) comprises reactor (21) and vavuum pump (22), and the charging aperture of reactor (21) and end not second pipeline (1221) of one group of water absorbing mechanism (1) connect, and vavuum pump (22) is connect by the 5th pipeline (221) and reactor (21).
2, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas is characterized in that described absorption tower (11) is waste gas absorption tower.
3, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas is characterized in that the reactor that described reactor (21) stirs for band.
4, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas, the quantity that it is characterized in that described water absorbing mechanism (1) is 2～5 groups.
5, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas, the quantity that it is characterized in that described water absorbing mechanism (1) is 2～4 groups.
6, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas, the quantity that it is characterized in that described water absorbing mechanism (1) is 3 groups, wherein, the 4th pipeline (132) of second group of water absorbing mechanism (1) is provided with first valve (4), and the 4th pipeline (132) of second group of water absorbing mechanism (1) connects with the storage tank (12) of first group of water absorbing mechanism (1) mutually by the 6th pipeline (5); The 4th pipeline (132) of the 3rd group of water absorbing mechanism (1) is provided with second valve (6), and the 4th pipeline (132) of the 3rd group of water absorbing mechanism (1) connects with the storage tank (12) of second group of water absorbing mechanism (1) mutually by the 7th pipeline (7).
7, the hydrogen chloride during lipoic acid according to claim 1 is produced and the retracting device of sulfur dioxide mix waste gas is characterized in that the vacuum of described vavuum pump (22) is-0.08～0.1MPa.
8, the hydrogen chloride during lipoic acid according to claim 7 is produced and the retracting device of sulfur dioxide mix waste gas is characterized in that the vacuum of described vavuum pump (22) is-0.09MPa.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100220542A CN101332408A (en) | 2008-06-24 | 2008-06-24 | Preparation method of DHA jellyfish egg polypeptides freeze-dry powder |
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2008100220542A CN101332408A (en) | 2008-06-24 | 2008-06-24 | Preparation method of DHA jellyfish egg polypeptides freeze-dry powder |
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| CN101332408A true CN101332408A (en) | 2008-12-31 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101810995A (en) * | 2010-04-16 | 2010-08-25 | 浙江巨化股份有限公司硫酸厂 | Comprehensive recycling system of chlorine-containing sulfur-containing tail gas and method |
| CN103111181A (en) * | 2012-05-07 | 2013-05-22 | 山东金城柯瑞化学有限公司 | Method for recycling tail gas of sulfonyl chloride chlorination in Cmoba synthesis |
| CN105327593A (en) * | 2015-11-12 | 2016-02-17 | 中国石油化工股份有限公司 | Hydrochloric acid treatment device and treatment method for ship loading operation |
| CN108744943A (en) * | 2018-07-25 | 2018-11-06 | 湖南天翊环保科技有限公司 | A kind of desulphurization plant and its sulfur removal technology |
| CN111185079A (en) * | 2019-12-04 | 2020-05-22 | 大连百傲化学股份有限公司 | Resourceful treatment method for acid gas in incineration flue gas |
-
2008
- 2008-06-24 CN CNA2008100220542A patent/CN101332408A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101810995A (en) * | 2010-04-16 | 2010-08-25 | 浙江巨化股份有限公司硫酸厂 | Comprehensive recycling system of chlorine-containing sulfur-containing tail gas and method |
| CN103111181A (en) * | 2012-05-07 | 2013-05-22 | 山东金城柯瑞化学有限公司 | Method for recycling tail gas of sulfonyl chloride chlorination in Cmoba synthesis |
| CN105327593A (en) * | 2015-11-12 | 2016-02-17 | 中国石油化工股份有限公司 | Hydrochloric acid treatment device and treatment method for ship loading operation |
| CN108744943A (en) * | 2018-07-25 | 2018-11-06 | 湖南天翊环保科技有限公司 | A kind of desulphurization plant and its sulfur removal technology |
| CN111185079A (en) * | 2019-12-04 | 2020-05-22 | 大连百傲化学股份有限公司 | Resourceful treatment method for acid gas in incineration flue gas |
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Open date: 20081231 |