CN1778352B - Chinese medicine composition for treating cardiovascular disease - Google Patents

Abstract

The invention discloses a medicine for treating coronary heart disease, which is prepared from salvia miltiorrhiza, red peony root and balsamic oil or styrax as raw materials. or alcohol extract; (2) carry out preliminary clarification treatment to described extract; (3) further carry out ultrafiltration to described extract; (4) concentrate ultrafiltrate, add balsamic oil or styrax according to routine Methods to make preparations.

Description

A kind of traditional Chinese medicine composition for treating cardiovascular disease

technical field

The invention relates to a traditional Chinese medicine prepared by an ultrafiltration process. Specifically, the present invention relates to a traditional Chinese medicine composition for treating cardiovascular diseases.

Background technique

Membrane separation technology (Membrane Separation Technique) is a new high-efficiency separation technology, which has been internationally recognized as the most promising high-tech production technology from the end of the 20th century to the middle of the 21st century. Ultrafiltration (UF) technology is a membrane separation technology whose basic principle is to use the selective screening performance of membrane pores to separate, purify and concentrate substances. The ultrafiltration method uses an anisotropic membrane (that is, an asymmetric membrane) made of polymer materials as the filter medium. Under normal temperature conditions, relying on a certain pressure and flow rate, the solution flows through the membrane surface, forcing low molecular weight substances to permeate. Through the membrane, the polymer substances are intercepted.

Because the ultrafiltration method is a physical method, it has the characteristics of no need for repeated heating, no "phase state" change, less possibility of destroying active ingredients than other general methods, and short process flow, so it is applied to the research of extracting active ingredients of traditional Chinese medicine Increasingly active, some products have moved from laboratory research to industrial production. People's Liberation Army 304 Hospital Wang Shiling and others used ultrafiltration to extract the active ingredient baicalin in Scutellaria baicalensis. The results showed that the ultrafiltration method was superior to the conventional method in terms of yield and purity, and one ultrafiltration can meet the requirements of injections without further steps. Refined, simple process, the production cycle can be shortened by 1 to 2 times (Wang Shiling, Zheng Dianbao "A Preliminary Investigation on the Extraction of Baicalin by Ultrafiltration", Chinese Patent Medicine Research, 1988 (3): 5). Wang Shiling and others have further studied the optimal process conditions for extracting baicalin by ultrafiltration. The experimental results prove that the selection of an ultrafiltration membrane with a suitable pore size (molecular weight cut-off is 6000-10000) is the key to improving the yield and quality of baicalin. Liquid temperature or lower concentration, strictly control the pH value (pH=1.5 during acidification, pH=7.0 during alkali dissolution), can significantly improve the ultrafiltration speed, and obtain the best output effect (Wang Shiling, "One-time extraction of baicalin by ultrafiltration Technology Research", Chinese Patent Medicine, 1994, 16(3): 2). Xu Jinlin and others used the ultrafiltration method (polysulfone membrane, molecular weight cut-off 6000) in the preparation of phytic acid, and the yield of phytic acid was 86.4%, which was 12.6% higher than the conventional phytate method, and the phytic acid obtained by the ultrafiltration method was almost It does not contain inorganic phosphorus, and its appearance is transparent and almost colorless (Xu Jinlin, Xu Jie, Wang Yuanjin "Research on Preparation of Phytic Acid by Membrane Separation Technology", China Journal of Pharmaceutical Industry, 1994, 25(4): 150). He Changsheng and others applied ultrafiltration technology to separate and refine stevioside, and used ultra-thin plate ultrafilter and cellulose acetate membrane (CA membrane) with a molecular weight cut-off of 10,000 to carry out field experiments on the purification of stevioside. The process flow is reasonable and feasible. The performance of the ultrafilter is stable, the decolorization performance of the membrane and the effect of removing impurities are good, which can better solve the problems of precipitation and foaming during potting that often occur in the production of stevioside (He Changsheng, Wang Bingnan, Zhu Shanshan "Stevioside Application Research of Ultrafiltration", Water Treatment Technology, 1994, 20(2): 89). Huang Ziqiang used ultrafiltration membranes (polysulfone membranes with a molecular weight cut-off of 4000 and 10000) to refine camellia oleifera saponin, compared with the bleaching method, recrystallization method, alcohol ether precipitation method and alkaline salt precipitation method mostly used in China, the ultrafiltration process flow Simple, efficient, low cost, to remove grease, pigments, sugars and other highly hydrophilic impurities in the crude camellia saponin, all can achieve the expected effect (Huang Ziqiang, "Ultrafiltration membrane method refining camellia saponin preliminary research" water Process Technology, 1995, 21(2):99). Guo Liwei from Nanjing University of Traditional Chinese Medicine compared and studied the effects of water-alcohol method and ultrafiltration method on the clarification of Cornus officinalis preparations on the ingredients contained in the preparations. Ultrafiltration membrane has no obvious effect on loganin (molecular weight is 384), but the film with molecular weight cut-off is 1000 makes loganin loss about 50% (Guo Liwei, Peng Guoping, Pan Yang et al. A Comparative Study of Chinese Medicine Preparations from Cornus officinalis", Chinese Patent Medicine, 1999, 21(2): 59). Wang Chengzhang et al. used ultrafiltration (polysulfone membrane, molecular weight cut-off 30000) and polyamide resin adsorption elution method to separate and purify the ethanol extract of Ginkgo biloba leaves, and the content of ginkgo flavonoid glycosides was detected by high performance liquid chromatography (HPLC). At about 45%, the yield is 0.5% to 0.7%, which is superior to conventional steam distillation and organic solvent extraction, and can reduce waste water discharge in the ultrafiltration process, protect the environment, reduce production costs, and improve economic benefits ( Wang Chengzhang, Yu Qing, Tan Weihong, etc. "Application of Ultrafiltration in the Purification of Ginkgo Flavonoid Glycosides", Forestry Science and Technology Communication, 1997, (2): 21).

Although the application of ultrafiltration technology in the production of traditional Chinese medicine preparations has its unique advantages, the extent of its application is still very limited. The reason is that there are still the following problems:

(1) The composition of Chinese herbal medicine is complex, especially in many compound preparations, the active ingredients have not been fully understood, so it needs to be thoroughly studied before applying ultrafiltration technology to Chinese herbal medicine preparations. For example, due to the complexity of the components, it is impossible to apply ultrafiltration to the production of most traditional Chinese medicine preparations before a large number of pharmacological and clinical research tests are conducted to fully evaluate the effect of ultrafiltration on the efficacy of each component in traditional Chinese medicine preparations.

(2) There are few types of membrane materials, the membrane pore size distribution is wide, and the performance is not stable. The ultrafiltration membrane materials used in the production of traditional Chinese medicine preparations include cellulose acetate, polyacrylonitrile, polysulfone, sulfonated polysulfone, polysulfone amide, etc. According to its affinity to water, it can be roughly divided into two categories: hydrophobic membrane materials and hydrophilic membrane materials. Hydrophilic membrane materials such as cellulose acetate and sulfonated polysulfone have less adsorption of solutes and a smaller molecular weight cut-off, but poor thermal stability, mechanical strength, chemical resistance, and bacterial erosion resistance are usually not high; polysulfone and other hydrophobic Membrane material has high mechanical strength, high temperature resistance, solvent resistance, and biodegradation resistance, but because the molecular chain contains a large number of hydrophobic genes or chain links, and has a lot of electrostatic charges, the membrane has a low water permeability and low anti-pollution ability .

(3) Membrane fouling is the biggest obstacle preventing ultrafiltration technology from laboratory research to industrial application. In the ultrafiltration process of traditional Chinese medicine preparations, if the pretreatment effect of the liquid medicine is not good, the membrane surface will be easily polluted and the membrane pores will be blocked, which will reduce the permeation flux, that is, the productivity, or even fail to work normally, reduce the production efficiency, and increase the cost, resulting in membrane shortened service life.

(4) The selection method of membrane modules has not been established yet, and the operating parameters of ultrafiltration still need to be optimized. There are many factors that affect the effect of ultrafiltration, including the selection of membrane components, the determination of process parameters and the cleaning method of the ultrafilter after use. Therefore, the ultrafiltration equipment and operating technology suitable for ultrafiltration of traditional Chinese medicine systems need further research.

After long-term and unremitting efforts, the inventor determined the appropriate process operating conditions by analyzing a large number of experimental data, and provided a specific solution for the industrial production of the drug of the present invention by ultrafiltration.

Contents of the invention

The purpose of the present invention is to provide a traditional Chinese medicine prepared by an ultrafiltration preparation process with less impurities, less active ingredient loss and low cost, which overcomes the deficiencies in the prior art and solves the difficult problem of the operability of industrial production ultrafiltration process conditions .

The present invention is realized through the following technical steps: using salvia miltiorrhiza, red peony root and balsamic oil as raw materials, it is prepared according to the following steps:

(1) Mix Salvia Miltiorrhiza and Radix Paeoniae Rubra or separately make water extract or alcohol extract;

(2) Carry out preliminary clarification treatment to described extract;

(3) further carry out ultrafiltration treatment to described extract;

(4) Concentrate the ultrafiltrate, add balsamic oil, and make a preparation according to a conventional method.

The weight percentage of above-mentioned crude drug is: Salvia miltiorrhiza 20%～97%, red peony root 2%～79%, balm oil 0.2%～3%; 0.5%-2.0% of sesame oil; more preferably 75.2%-90% of salvia miltiorrhiza, 9%-23.5% of red peony root, and 0.5%-1.3% of balm oil. The sum of the percentages by weight of salvia miltiorrhiza, red peony root and balsamic oil is 100%.

The above-mentioned raw material Dalbergia can be replaced by Styrax, that is, the above-mentioned raw material can be 20%-97% of Salvia miltiorrhiza, 2%-79% of Radix Paeoniae Rubra, 0.2%-3% of Stellaris; preferably 63.0%-94% of Salvia Miltiorrhiza and 4.0% % to 35.0%, styrax 0.5% to 2.0%; more preferably Danshen 75.2% to 90%, red peony 9% to 23.5%, styrax 0.5% to 1.3%. The sum of the percentages by weight of salvia miltiorrhiza, red peony root and styrax is 100%.

In the technical step (1) of the present invention, the alcohol extract can be lower alcohols of different concentrations such as methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol, etc., or extracts of their mixtures. The alcohol extract can be subjected to the next preliminary clarification treatment without concentration or after proper concentration.

In the technical step (2) of the present invention, preliminary clarification treatment can carry out rough filtration with general material such as gauze, silk silk etc., also can carry out microfiltration with more professional material such as ceramic membrane, also can get supernatant after high-speed centrifugation Liquid, also can use flocculant such as chitosan flocculation clarifier, 101 fruit juice clarifier, ZTC1+1 natural clarifier, egg white flocculant etc. Some impurities. The above clarification methods can be used alone or in combination, such as coarse filtration-adsorption clarification, adsorption clarification-high-speed centrifugation, coarse filtration-microfiltration, coarse filtration-alcohol precipitation, etc. The solution that has been preliminarily clarified can be subjected to the next step of ultrafiltration without concentration or after being properly concentrated; preferably, the next step of ultrafiltration is performed without concentration.

In the technical step (3) of the present invention, the ultrafiltration membrane used for ultrafiltration can be cellulose diacetate membrane (CA), cellulose triacetate membrane (CTA), cyanoethyl cellulose acetate membrane (CN-CA), polyester Sulfone membrane (PS), sulfonated polysulfone membrane (SPS), polyethersulfone membrane (PES), sulfonated polyethersulfone membrane (SPES), polysulfone amide membrane (PSA), phenolphthalein side group polyarylsulfone membrane (PDS) ), polyvinylidene fluoride film (PVDF), polyacrylonitrile film (PAN), polyimide film (N), cellulose film, methyl methacrylate-acrylonitrile copolymer film (MMA-AN), poly Acrylonitrile/cellulose diacetate (PAN/CA) blend membranes, dynamically formed ultrafiltration membranes, and modified membranes of the above membranes. Preferably cellulose diacetate membrane (CA), cellulose triacetate membrane (CTA), polysulfone membrane (PS), sulfonated polysulfone membrane (SPS), polyethersulfone membrane (PES), sulfonated polyethersulfone membrane (SPES), polysulfoneamide membrane (PSA), polyvinylidene fluoride membrane (PVDF), polyacrylonitrile membrane (PAN).

The molecular weight cut-off of the ultrafiltration membrane is generally 6000-80000, preferably 10000-70000, most preferably 20000-50000.

Ultrafiltration can be either cross-flow filtration or dead-end filtration, but cross-flow filtration is preferred.

The operating conditions of the ultrafiltration process are as follows:

(1) The inlet pressure of the ultrafiltration is 0.1-0.5MPa, preferably 0.1-0.35Mpa, and most preferably 0.25-0.35Mpa; the outlet pressure of the ultrafiltration is 0.5-0.25kPa lower than the inlet pressure. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.1-0.2Mpa.

(2) The flow rate of the feed liquid is 1.0-4.0 m/s, preferably 2.0-3.0 m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unsteady flow in the membrane channel, and the flow velocity fluctuation difference is 1.0-2.0m/s.

(3) In the ultrafiltration system, high-pressure inert gas such as nitrogen is fed intermittently to form a gas-liquid pulse flow, and the cycle is 0.5h-2h to ventilate once, each time for 1 minute.

(3) The feed liquid temperature is 15-50°C, preferably 20-40°C.

(4) When the stock solution is concentrated by 1/15 to 1/5, add water or dilute alcohol solution for ultrafiltration 1 to 2 times; preferably when the stock solution is concentrated by 1/12 to 1/8, add water Or dilute alcohol solution ultrafiltration 1 to 2 times.

(5) The pH value of the feed liquid is controlled at 5 to 9, preferably 6.0 to 7.5;

(6) Backwashing conditions: Backwashing pressure is 0.15-2.5MPa, backwashing cycle is 0.5-1.5h, and backwashing time is 1min-10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time To carry out, generally work for 10 to 20 minutes, and recoil for 30 seconds to 3 minutes.

(7) The chemical cleaning period is 0.5 months to February. The chemical cleaning agents are generally dilute acids, dilute alkalis, and surfactants, preferably dilute alkalis, such as 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2 % sodium hypochlorite mixed solution, etc., the pH value is 10-12, and the cleaning working pressure is 0.05-1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

In the ultrafiltration process, periodic pressure fluctuations or periodic flow fluctuations or periodic inert gas injections can be used alone, or in combination, that is, periodic pressure fluctuations and periodic flow fluctuations are used in combination, or periodic pressure fluctuations It is used in combination with periodic inert gas injection, or in combination with periodic flow fluctuations and inert gas injection, or in combination with the three.

In the technical step (4) of the present invention, after the ultrafiltrate is concentrated into an extract, the preparation is then prepared in a conventional manner. For example, it can be mixed with any one or more pharmaceutical excipients such as starch, dextrin, lactose, microcrystalline cellulose, hydroxypropylmethylcellulose, polyethylene glycol, magnesium stearate, micronized silica gel, xylose Alcohol, lactitol, glucose, glycine, mannitol, glycine, etc. are mixed to form tablets, capsules, granules, oral liquids, sustained-release preparations, controlled-release preparations, gels, ointments, ointments, creams, suppositories , injections, powder injections, patches, dripping pills, suspensions, etc.

Experimental Example Clinical Observation on Drug Treatment of Coronary Heart Disease of the Present Invention

1. General information: According to the 1976 WHO diagnostic criteria for coronary heart disease, 30 cases were selected to take the medicine of the present invention as the treatment group, and 30 cases were taken as the control group to be treated with Xiaoxintong for observation. In the treatment group, there were 24 males and 6 females, aged 55 to 80 years, with a course of 1 to 10 years, including 24 cases of stable angina, 6 cases of unstable angina, 7 cases of hypertension and 3 cases of diabetes. In the control group, there were 23 males and 7 females, aged 52-78 years, with a course of 1-9 years, including 25 cases of stable angina, 5 cases of unstable angina, 8 cases of hypertension and 2 cases of diabetes.

2. Test method: the treatment group took the medicine of the present invention orally, 3 tablets at a time, 3 times a day; the control group took 10 mg of Xiaoxintong orally, 3 times a day. The course of treatment for the two groups was 4 weeks. Patients with high blood pressure and diabetes continued to take antihypertensive and hypoglycemic drugs for treatment. If angina pectoris occurs during the medication, take nitroglycerin temporarily. Before treatment, during treatment and after treatment, the number of angina pectoris attacks, pain conditions, times of nitroglycerin, blood sugar, liver function, BUN and electrocardiogram, blood pressure were recorded, and adverse reactions after taking the medicine were recorded.

3. Judgment criteria for curative effect:

3.1 Symptoms of angina pectoris Markedly effective: angina pectoris basically disappears without nitroglycerin; effective: the number of angina pectoris attacks and the dosage of nitroglycerin are halved; ineffective: the number of angina pectoris is basically not relieved or the number of attacks is reduced by less than half; exacerbation: the number of angina pectoris attacks and the dosage of nitroglycerin are increased.

3.2 Electrocardiogram Significantly effective: resting ischemic electrocardiogram returned to normal or roughly normal after treatment; effective: S-T segment rebounded by about 0.05mv, T wave inversion became shallower by more than 50% or turned from flat to upright; invalid; S-T segment, T wave Changes without improvement; aggravated: S-T segment, T wave changes aggravated.

4. Results:

4.1 The total effective rate of treatment of angina pectoris symptoms in the two groups (marked effect plus effective)

The treatment group was 83.33%, and the control group was 80%. The P value of the curative effect of the two groups was tested by ^X2 , and there was no significant difference.

4.2 The total effective rate of resting ischemic electrocardiogram improvement in the two groups of patients (marked effect plus effective)

The treatment group was 60%, and the control group was 56.67%. The curative effect of the two groups was P>0.05 by ^X2 test, and there was no significant difference. The heart rate, liver function, and BUN of the two groups were normal before and after treatment, and had no effect on blood pressure and blood sugar. The treatment group had no adverse reactions during the treatment period.

Table 1 Analysis of curative effect of 30 cases of coronary heart disease with angina pectoris

Table 2 Analysis of the curative effect of resting ischemic electrocardiogram in 30 patients with coronary heart disease and angina pectoris

Detailed ways

The present invention will be further elaborated below in conjunction with embodiment. These examples are for illustrative purposes only and do not limit the invention in any way.

Embodiment one

The raw materials are 450g of Salvia miltiorrhiza, 141g of red peony root, and 8g of balsamic oil.

Extract Danshen with ethanol to obtain ethanol extract of Danshen, filter the extract with gauze, and collect the filtrate. The filtrate was ultrafiltered with a cellulose diacetate membrane with a molecular weight cut-off of 6000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.1Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.5kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are used, and the pressure fluctuation difference is 0.1Mpa. The flow rate of the feed liquid is 1.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 1.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 0.5h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 15°C. When the original feed liquid is concentrated by 1/15, add water or dilute alcohol solution for ultrafiltration once, and the pH value of the feed liquid is controlled at 5. The backwash pressure is 0.15MPa, the backwash cycle is 0.5h, and the backwash time is 1min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 10min, recoil for 30sec. The chemical cleaning cycle is 0.5 months, the chemical cleaning agent is a mixed solution of 0.5%-4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10-12, and the cleaning working pressure is 0.05MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind Radix Paeoniae Rubra into fine powder, mix with Danshen extract, dry, make granules, spray into balsamic oil, mix with the above granules, press into 1000 tablets, coat with sugar, and get ready.

Embodiment two

The raw materials are 558g of Salvia miltiorrhiza, 34g of red peony root, and 8g of balsamic oil.

Extracting Danshen with ethanol to obtain the ethanol extract of Danshen, microfiltration with ceramic membrane, and collecting the filtrate. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 80,000, and the filtration method was dead-end filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.5Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.25kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 4.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 50°C. When the raw liquid of the feed liquid is concentrated by 1/5, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 9. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind Radix Paeoniae Rubra into fine powder, mix with Danshen extract, dry, make granules, spray into balsamic oil, mix with the above granules, add 3% povidone ethanol solution to make soft material, pass through 18-mesh sieve to make granules , dried at 60°C for 30-45 minutes, granulated, added with talcum powder, mixed evenly, filled in capsules, and obtained.

Embodiment three

The raw materials are 360g of Salvia miltiorrhiza, 232g of red peony root, and 8g of balsamic oil.

The ethanol extract of Salvia miltiorrhiza was obtained by extracting the salvia miltiorrhiza with ethanol, the extract was centrifuged at high speed and the supernatant was collected. The liquid is ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 50,000, and the filtration method adopts cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.35Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.20kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 3.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating or unstable flows in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 40°C. When the original feed liquid is concentrated by 1/8, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 7.5. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind red peony root into fine powder, mix with salvia miltiorrhiza extract, dry, make granules, spray with baldwood oil, mix with the above granules, press into 1000 tablets, or coat with sugar.

Embodiment four

The raw materials are 500 grams of Danshen, 94 grams of Radix Paeoniae Rubra, and 6 grams of balsamic oil.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a cellulose diacetate membrane with a molecular weight cut-off of 6000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.1Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.5kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are used, and the pressure fluctuation difference is 0.1Mpa. The flow rate of the feed liquid is 1.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 1.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 0.5h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 15°C. When the original feed liquid is concentrated by 1/15, add water or dilute alcohol solution for ultrafiltration once, and the pH value of the feed liquid is controlled at 5. The backwash pressure is 0.15MPa, the backwash cycle is 0.5h, and the backwash time is 1min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 10min, recoil for 30sec. The chemical cleaning cycle is 0.5 months, the chemical cleaning agent is a mixed solution of 0.5%-4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10-12, and the cleaning working pressure is 0.05MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32 to 1.40 (55° C.), spray it with balm oil, mix evenly, fluidize with lactose in a batch fluidized bed, dry, and make granules, namely have to.

Embodiment five

The raw materials are 290 grams of Salvia miltiorrhiza, 306 grams of red peony root, and 6 grams of balsamic oil.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 80,000, and the filtration method was dead-end filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.5Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.25kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 4.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 50°C. When the raw liquid of the feed liquid is concentrated by 1/5, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 9. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32 to 1.40 (55°C), mix the extract with an appropriate amount of magnesium stearate, spray it with balm oil, mix it with the above granules, and press it into Tablets, film-coated.

Embodiment six

The raw materials are 210 grams of Salvia miltiorrhiza, 380 grams of red peony root, and 4 grams of balsamic oil.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 50,000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.35Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.20kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 3.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating or unstable flows in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 40°C. When the original feed liquid is concentrated by 1/8, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 7.5. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32 to 1.40 (55°C), mix the extract with an appropriate amount of magnesium stearate, spray it with balm oil, mix it with the above granules, and press it into tablet.

Embodiment seven

The raw materials are 450g of Danshen, 141g of Radix Paeoniae Rubra, and 8g of Styrax.

Extract Danshen with ethanol to obtain ethanol extract of Danshen, filter the extract with gauze, and collect the filtrate. The filtrate was ultrafiltered with a cellulose diacetate membrane with a molecular weight cut-off of 6000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.1Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.5kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are used, and the pressure fluctuation difference is 0.1Mpa. The flow rate of the feed liquid is 1.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 1.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 0.5h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 15°C. When the original feed liquid is concentrated by 1/15, add water or dilute alcohol solution for ultrafiltration once, and the pH value of the feed liquid is controlled at 5. The backwash pressure is 0.15MPa, the backwash cycle is 0.5h, and the backwash time is 1min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 10min, recoil for 30sec. The chemical cleaning cycle is 0.5 months, the chemical cleaning agent is a mixed solution of 0.5%-4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10-12, and the cleaning working pressure is 0.05MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind red peony into fine powder, mix with Danshen extract, dry, make granules, add Styrax, mix evenly, press into 1000 tablets, coat with sugar, and get ready.

Embodiment Eight

The raw materials are 558g of Danshen, 34g of Radix Paeoniae Rubra, and 8g of Styrax.

Extracting Danshen with ethanol to obtain the ethanol extract of Danshen, microfiltration with ceramic membrane, and collecting the filtrate. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 80,000, and the filtration method was dead-end filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.5Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.25kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 4.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 50°C. When the raw liquid of the feed liquid is concentrated by 1/5, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 9. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind Radix Paeoniae Rubra into fine powder, mix with Salvia Miltiorrhiza Extract, grind Styrax into fine powder, mix with the above granules, add 3% povidone ethanol solution to make soft material, pass through 18 mesh sieve to make granules, dry at 60°C for 30~ After 45 minutes, whole grains, add talcum powder, mix well, fill in capsules, and get ready.

Embodiment nine

The raw materials are 360g of Danshen, 232g of Radix Paeoniae Rubra, and 8g of Styrax.

The ethanol extract of Salvia miltiorrhiza was obtained by extracting the salvia miltiorrhiza with ethanol, the extract was centrifuged at high speed and the supernatant was collected. The liquid is ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 50,000, and the filtration method adopts cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.35Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.20kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 3.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating or unstable flows in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 40°C. When the original feed liquid is concentrated by 1/8, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 7.5. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrating the ultrafiltrate to obtain the salvia miltiorrhiza extract with a relative density of 1.35-1.39 (55° C.). Grind red peony root into fine powder, mix with salvia miltiorrhiza extract, dry, make granules, add styrax, mix well, press into 1000 tablets, or coat with sugar, to get ready.

Embodiment ten

The raw materials are 500 grams of Danshen, 94 grams of Radix Paeoniae Rubra, and 6 grams of Styrax.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a cellulose diacetate membrane with a molecular weight cut-off of 6000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.1Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.5kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are used, and the pressure fluctuation difference is 0.1Mpa. The flow rate of the feed liquid is 1.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 1.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 0.5h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 15°C. When the original feed liquid is concentrated by 1/15, add water or dilute alcohol solution for ultrafiltration once, and the pH value of the feed liquid is controlled at 5. The backwash pressure is 0.15MPa, the backwash cycle is 0.5h, and the backwash time is 1min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 10min, recoil for 30sec. The chemical cleaning cycle is 0.5 months, the chemical cleaning agent is a mixed solution of 0.5%-4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10-12, and the cleaning working pressure is 0.05MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32-1.40 (55° C.), add styrax, mix evenly, fluidize with lactose in a batch fluidized bed, dry, and make granules.

Embodiment Eleven

The raw materials are 290 grams of Danshen, 306 grams of Radix Paeoniae Rubra, and 6 grams of Styrax.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 80,000, and the filtration method was dead-end filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.5Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.25kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 4.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating flow or unstable flow in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 50°C. When the raw liquid of the feed liquid is concentrated by 1/5, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 9. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32-1.40 (55°C), add styrax, add 30 g of mannitol, 5 g of calcium sodium edetate, and 5 ml of distilled water, mix the above components, and freeze Dry, sub-package, that is.

Embodiment 12

The raw materials are 210 grams of Danshen, 380 grams of Radix Paeoniae Rubra, and 4 grams of Styrax.

Put the coarsely crushed salvia miltiorrhiza and red peony into the extraction tank, add 5 times the amount of water, decoct for 2 hours, filter, and extract the filter residue for the second time, add 4 times the amount of water, fry for 1 hour, filter, and discard the filter residue To, combine the filtrates. The filtrate was ultrafiltered with a polysulfone membrane with a molecular weight cut-off of 50,000, and the filtration method was cross-flow filtration. The operating conditions of the ultrafiltration process are: the pressure of the liquid inlet of the ultrafiltration is 0.35Mpa, and the pressure of the liquid outlet of the ultrafiltration is 0.20kPa lower than the pressure of the liquid inlet. In the initial stage of ultrafiltration, a lower pressure is used, and then the pressure is gradually increased; in the process of ultrafiltration, periodic pressure fluctuations are adopted, and the pressure fluctuation difference is 0.2Mpa. The flow rate of the feed liquid is 3.0m/s. During the ultrafiltration process, periodic flow fluctuations are used to generate pulsating or unstable flows in the membrane channel. The difference in flow rate fluctuations is 2.0m/s. Nitrogen is intermittently fed into the ultrafiltration system , to form a gas-liquid pulse flow, and the period is 2h to ventilate once, each time for 1 minute. The temperature of the feed liquid is 40°C. When the original feed liquid is concentrated by 1/8, add water or dilute alcohol solution for ultrafiltration twice, and the pH value of the feed liquid is controlled at 7.5. The backwash pressure is 2.5MPa, the backwash cycle is 1.5h, and the backwash time is 10min. When the ultrafiltration modules are connected in parallel to use the method of alternate backflushing, one or several sets perform normal ultrafiltration and part of the filtrate is flowed out to backwash the ultrafiltration membrane of another set or several sets of components, and exchange after a period of time Carry out, work for 20 minutes, recoil for 3 minutes. The chemical cleaning cycle is 2 months, the chemical cleaning agent is a mixed solution of 0.5% to 4.0% sodium hydroxide, 1.5% sodium hydroxide and 2% sodium hypochlorite, the pH value is 10 to 12, and the cleaning working pressure is 1.0MPa. After cleaning with chemical cleaners, rinse with water until nearly neutral.

Concentrate the ultrafiltrate to obtain an extract with a relative density of 1.32-1.40 (55° C.), mix the extract with an appropriate amount of magnesium stearate, add styrax, mix evenly, and press into tablets.

Claims (12)

1. A traditional Chinese medicine composition for the treatment of coronary heart disease angina pectoris, characterized in that it is prepared from the following raw materials in percentage by weight: Salvia miltiorrhiza 20% to 97%, Radix Paeoniae Rubra 2% to 79%, Dalbergia oil or Styrax 0.2% ~3%; Its preparation method is: (a) mixing salvia miltiorrhiza and red peony root or making water extract or alcohol extract separately; (b) Carrying out preliminary clarification treatment to the extract; (c) further carrying out ultrafiltration to the extract; (d) Concentrate the ultrafiltrate, add balsamic oil or styrax, and make a preparation according to a conventional method; The operation process condition of described ultrafiltration treatment is as follows: The liquid inlet pressure of ultrafiltration is 0.1-0.5MPa, and the liquid outlet pressure of ultrafiltration is 0.25-0.5kPa lower than the liquid inlet pressure; the temperature of the feed liquid is 15-50°C; the pH value of the feed liquid is controlled at 5-9 ; When the feed solution is concentrated by 1/15 to 1/5, add water or dilute alcohol solution for ultrafiltration 1 or 2 times; In the ultrafiltration process, the following methods are used alone or in combination: periodic pressure fluctuations, periodic flow fluctuations, and intermittent inert gas injection; wherein the pressure fluctuation difference of the periodic pressure fluctuations is 0.1 to 0.2Mpa, and the periodic flow rate The fluctuating flow rate fluctuation difference is 1.0-2.0 m/s, and the inert gas is intermittently fed in every 0.5-2 hours for 1 minute each time. 2. Chinese medicine composition as claimed in claim 1, is characterized in that the weight percent of described raw material is: Salvia miltiorrhiza 63.0%～94%, Radix Paeoniae Rubra 4.0%～35.0%, Falling oil or styrax 0.5% to 2.0%. 3. Chinese medicine composition as claimed in claim 2 is characterized in that the weight percent of described raw material is: Danshen 75.2% ~ 90%, Radix Paeoniae Rubra 9%～23.5%, Falling oil or styrax 0.5% to 1.3%. 4. Chinese medicine composition as claimed in claim 1, is characterized in that described ethanol extract is the extract that is selected from following lower alcohol or its mixture: methyl alcohol, ethanol, n-propanol, isopropanol, n-butyl alcohol alcohol, isobutanol. 5. The Chinese medicine composition as claimed in claim 1, characterized in that said alcohol extract is an ethanol extract. 6. The Chinese medicine composition as claimed in claim 1, characterized in that what is obtained in said step (a) is the ethanol extract of Salvia Miltiorrhiza. 7. The Chinese medicine composition as claimed in claim 1, characterized in that what is obtained in the step (a) is the water extract prepared by mixing Salvia miltiorrhiza and Radix Paeoniae Rubra. 8. The traditional Chinese medicine composition according to claim 1, characterized in that the preliminary clarification treatment is coarse filtration-adsorption clarification, adsorption clarification-high-speed centrifugation, coarse filtration-microfiltration or coarse filtration-alcohol precipitation. 9. The Chinese medicine composition according to claim 1, wherein the ultrafiltration membrane used in the ultrafiltration treatment is selected from the group consisting of: polysulfone membrane, sulfonated polysulfone membrane, polyethersulfone membrane, sulfonated polyethersulfone membrane , polysulfone amide membrane, polyarylsulfone membrane with phenolphthalein side group, polyvinylidene fluoride membrane, polyacrylonitrile membrane, polyimide membrane, cellulose membrane, methyl methacrylate-acrylonitrile copolymer membrane, polyacrylonitrile Cellulose/diacetate blend membrane, a dynamically formed ultrafiltration membrane, and a modified membrane of the above membrane; the molecular weight cut-off of the ultrafiltration membrane is 6,000 to 80,000. 10. The traditional Chinese medicine composition according to claim 9, wherein the cellulose film is a cellulose diacetate film, a cellulose triacetate film, or a cyanoethyl cellulose acetate film. 11. The traditional Chinese medicine composition according to claim 9 or 10, wherein the ultrafiltration membrane is selected from the group consisting of: polysulfone membrane, sulfonated polysulfone membrane, polyethersulfone membrane, sulfonated polyethersulfone membrane, polysulfone Amide membrane, polyvinylidene fluoride membrane, polyacrylonitrile membrane; the molecular weight cut-off of the ultrafiltration membrane is 10,000-70,000. 12. The traditional Chinese medicine composition as claimed in claim 1, characterized in that the preparation contains any one or more pharmaceutical excipients selected from the following: starch, dextrin, lactose, microcrystalline cellulose, hypromellose Cellulose, Polyethylene Glycol, Magnesium Stearate, Micronized Silica Gel, Xylitol, Lactitol, Glucose, Mannitol, Glycine.